CN1761588A - Thermodynamic cycles using thermal diluent - Google Patents

Abstract

Thermodynamic cycles with diluent that produce mechanical power, electrical power, and/or fluid streams for heating and/or cooling are described. Systems contain a combustion system producing an energetic fluid by combusting fuel with oxidant. Thermal diluent is preferably used in the cycle to improve performance, including one or more of power, efficiency, economics, emissions, dynamic and off-peak load performance, temperature regulation, and/or cooling heated components. Cycles include a heat recovery system and preferably recover and recycle thermal diluent from expanded energetic fluid to improve cycle thermodynamic efficiency and reduce energy conversion costs. Cycles preferably include controls for temperatures, pressures, and flow rates within a combined heat and power (CHP) system, and controls for power, thermal output, efficiency, and/or emissions.

Description

Use the thermodynamics circulation of hot diluent

                         Background of invention

Invention field

The present invention relates generally to the method for carrying out for generation of the thermodynamics circulation of mechanical energy and electric energy, heating or cooling.

The explanation of association area

Prior art comprises burner and the combustion system of cooling off combustion process with diluent, and it is relatively poor to peak temperature control, and the space of carrying out of almost can not distribute to transverse temperature (profile) is controlled. Usually use excess air that combustion product is cooled off. Compress the 40-70% (from large-scale turbine to miniature turbine) that these excess airs will consume the turbine general power of recovery usually and cause lower clean specific power. That is the compressor that the unit mass flow by this (a bit) compressor or turbine produces and the general power of pump power are lower.

The relevant application of diluent concentrates on especially controls discharging, flame holding and quenching of flame, particularly when use ultra-poor (ultra-lean) mixture and when operating near the combustion limits place (for example, referring to Lefebvre, 1998,5-7-3 joint; Bathie, 1996, p 139; Boyce, 2002, p 62; Lundquist, 2002, p 85). Some are attempted to reduce trial that excess air uses as diluent and have adopted hot diluent form such as steam and water, and it can take away the more heat (United States Patent (USP) the 3rd, 651 of Ginter for example by work done during compression still less, 641,5,627,719,5,743,080 and 6,289, No. 666, the United States Patent (USP) the 5th, 271 of Guillet, No. 215, No. the 6th, 370,862, the United States Patent (USP) of Cheng).

The temperature control of whole thermodynamics circulation is significant to effective running. The peak temperature of the high-energy fluid that is transported to decompressor and temperature distributed to control to make described circulation have better efficient (Gravonvski, 2001). Being difficult to control described temperature by the excess air that is generally used for cooling off circulation assembly and specific mixing arrangement or steam distributes. The scrambling that the room and time of fluid temperature (F.T.) distributes needs larger design margin, (the Malecki et al for example of preferred design margin when it surpasses the uncertainty that described temperature is distributed and compensates, " Application of and Advanced CFD-Based Analysis System to the PW600 Combustor to Optimize Exit Temperature Distribution-Part 1 ", 2001). The variation of workload can increase the weight of the problem of temperature scrambling.

Propose various thermodynamics and circulated to strengthen recuperation of heat and system effectiveness. The conventional circulation (Combined Cycle, CC) of uniting utilizes recuperation of heat steam generator (HRSG) to produce steam, and this steam expands by second (steam) turbine. This causes capital cost higher. Therefore, uniting circulation uses in foundation load is used usually. In steam re-injection formula gas turbine (STIG) circulation, in similar HRSG, produce steam and inject the upstream of decompressor. This has used has the more same gas turbine of high quality stream. Because described STIG circulation can only be carried steam, therefore reclaims the limited in one's ability of low temperature heat energy. It has been generally acknowledged that higher cost of water treatment and water conservancy expenditure are the major obstacles of the further extensive use of STIG. The CHENG circulation is similar with the STIG circulation. As the STIG circulation, also there is similar defective in it.

Recycled water injects (Recuperated Water Injection, RWI) recycling regenerative apparatus (recuperator) heat is reclaimed the fluid of the compression that is transferred to input from expansion fluid. This entrance that circulates in described regenerative apparatus adopts water to inject to improve recuperation of heat. This is subject to the limit of saturation of air equally. Humid air turbine (Humidified Air Turbine, HAT) cycles through saturator moisturizes the air of input. Evaporation formula gas turbine (Evaporated Gas Turbine, EvGT) is similar circulation. Although can utilize low-qualityer water, since the air saturation restriction, the limited amount of the diluent that described HAT and EvGT circulation can be carried. Carried out the checking of EvGT circulation in the LUND of Sweden university. Yet these RWI, HAT and EvGT circulation seldom are applied, and its reason may be that capital cost is higher. Once suggestion utilizes HAWIT to circulate to reduce capital cost. It adopts direct heat exchanger to reduce the cost of the surface heat exchanger that adopts in the HAT circulation. Compare with the HAT circulation, its cost is lower but efficient is also lower. Traverso (2000) compares relative efficiency and the internal rate of return (IRR) (rate of return) of these circulations.

Conventional recuperation of heat method is difficult to reclaim the effective heat energy that is lower than vapor (steam) temperature, and described steam is produced, had enough pressure to be recycled into the upstream of decompressor by expansion fluid, perhaps is arranged in the steam expansion machine. Because the steam after expanding is discharged from, therefore constantly lose a large amount of heat energy. Reclaiming the conventional method of heat energy from expansion fluid (the high-energy fluid expansion of heat discharges after the mechanical energy) attempts to adopt the high temperature regenerative apparatus to heat a large amount of excessive cooling air usually. For example, to the air of air backheating device near 700 ℃. This causes higher cost and expensive maintenance cost, and the individual cost of wherein said regenerative apparatus just surpasses 30% of small-sized turbine system cost, and maintenance cost then surpasses 80%.

In the relevant circulation such as " wetting " circulation (such as STIG and HAT) for generation of energy, use air diluent in addition to cause extra diluent supply and the expense of recovery. Relevant circulation with conventional heat and diluent recovery system usually needs to add " compensation " diluent and compensates the inefficient of described system and reduce running cost.

Because pollute and/or economic reason, except the fluid that contains oxidant, also use the thermodynamics circulation of diluent usually all to need this hot diluent is reclaimed. (for example, the italian patent TO92A000603 of Poggio and Agren number " Advanced Gas Turbine Cycles with Water-Air Mixtures as Working Fluid ", 2000). This class process is very expensive. Because the efficient of described removal process is lower, therefore usually all need to compensate diluent (Blanco, 2002).

Except when the hot diluent of adding, need to carry out the fluid filtration and purify preparing the diluent (Agren that is about to be transported to the described thermodynamics circulatory system, " Advanced Gas Turbine Cycles with Water-Air Mixtures as Working Fluid ", 2000; SPE " Mashproekt ", " Aquarius Cycle ", http://www.mashproekt.nikolaev.ua). This class conventional method has increased overspending.

Pollutant is just becoming whole world question of common concern, and it is controlled also more and more important. The method that adds entry of prior art has been aggravated the formation of some pollutant usually, for example when reducing other pollutant. (for example, referring to Lefebvre, 1998, p 337 is about CO vs NOx). The method that the control pollutant reaches the strict demand of rules needs extra assembly usually, causes a large amount of additional investments and maintenance cost. All be less than the life-span of whole equipment the service life of many these pollutant control device, thereby need extra maintenance cost. The excess air that main company all is devoted to be converted to drying reduces the NOx discharging, and avoids using steam as diluent.

Lefebvre (1998, p 337) proves that conventional thought do not encourage water is injected the turbo-power system. The cost that it has been generally acknowledged that water supply and processing is main obstacle. Commentator's prediction is along with the water or the steam that add circulation increase Efficiency Decreasing (Pavri and Moore 2001, p 18).

Sometimes thermodynamics is cycled to used in and carries out simultaneously mechanical work done and heating. The heat that is produced by combustion process can be used as from producing steam to the heat energy of the various application of district heating. The application of these " cogeneration of heat and power (CHP) " is subject to the restriction of CHP device design. If heat and the demand of power have been departed from the design load of described CHP system, then efficient significantly reduces, when particularly providing hot water.

                       Summary of the invention

To the circulation of many energy conversion systems and thermodynamics, all need to reduce cost and the discharging of the life cycle of system, and strengthen the property and reliability. Similarly, also need to improve thermodynamic efficiency, reduce maintenance cost and keep and improve because the restriction that equipment, environment cause comprises turbine blade life-span and pollutant emission.

Therefore, one embodiment of the invention comprise the thermodynamics power cycle with heat and quality transmission system that configuration is new, and this system can more effectively reclaim heat from the high-energy fluid that expands. In this class embodiment, the user preferably disposes the VAST circulation that energy conversion system strengthens with operation, thereby utilizes the diluent that comprises the component (such as water) of can vaporizing to come effectively to reclaim heat from the high-energy fluid of the expansion in decompressor downstream. In one embodiment, VAST-W cycles through the heating liquid diluent to reclaim heat from described expansion fluid, for example by water. In another embodiment, heating, evaporation liquid diluent are passed through in VAST steam circulation (VAST-WS), and preferably by making the overheated heat that reclaims of liquid diluent. For example by water and steam.

In other embodiments, be configured to use regenerative apparatus and VAST-W and VAST-WS assembly together heat to be recovered to from the expansion fluid of a part in the fluid that contains oxidant of input VAST backheat water-steam circulation (VAST-WSR). Every kind of circulation all comprises burner, and it preferably can operate to carry, mix and the oxidiferous fluid of fuel, contain the fluid of fuel, and one of the diluent of liquid diluent and vaporization or both.

In another embodiment, purpose is to cool off to reclaim heat from heat generating component and to hot assembly. In this embodiment, the user preferably distributes to reclaim heat from one or more hot assemblies and heat generating component to diluent, and these assemblies are one or more turbines, burner, generator, driver and motor for example. They preferably are equipped with controller, and this controller can operate to control diluent and distribute that a plurality of fluids and a plurality of assembly are cooled off, and the diluent of heat is transported to burner.

In certain embodiments, the VAST burner preferably is equipped with, it is set to and can loops control to VAST under near stoichiometric condition, the pollutant emission that keep to reduce simultaneously is such as described in the people's such as the people's such as the patent of Ginter, Hagen three fluids (Trifluid) patent application and Hagen ' 191 patent application. They preferably are configured to hold required all liquid diluents that are positioned at the decompressor upstream and/or diluent steam, thereby move under near stoichiometric condition. For example, add the diluent (for example water and steam) that is enough to surpass following one or more restrictions, these are restricted to air saturation restriction, steam produces restriction, and conventional pre-mixing combustion or flame holding restriction and droplet burn and extinguish restriction. Preferred relatively turbine is adjusted the size of compressor, to adapt to the lower flow that contains oxidant, saves great amount of cost.

In certain embodiments, a purpose is the cost that reduces supply and process the diluent in the described circulation. In this class embodiment, preferably with condenser expansion fluid is cooled off, and diluent is carried out condensation and recovery. The preferred direct contact type condenser that adopts cold diluent (water) that uses improves organic efficiency and minimizing pollutant emission. The water that preferred recovery combustion process forms and/or the diluent of airborne wet steam and injection, thus make the described water aspect energy self-sufficiency that circulates in. Reclaiming excessive diluent helps to discharge to take out fluid alloy (contaminant) by fluid. Preferably reduce the alloy of the flow introducing that contains oxidant of input with corresponding reduction method. By clean fuel and input spraying cleaning, can discharge controlled doping thing level by diluent. Described circulation is preferably processed and is re-used diluent, reduces processing cost.

In another embodiment, purpose is to improve heat to mechanical transformation of energy. In this class embodiment, the pressure ratio of compressor rises, and particularly adopts liquid diluent to carry. The user is preferably at the downstream of condenser and decompressor configuration recompression machine (recompressor). Can described burner be set to for reducing pressure drop. Can reduce the pressure loss in the described condenser with the direct contact type compressor. Described entrance compressor, recompression machine, the described burner pressure loss and direct contact loss are set realize the clean expansion ratio of the described turbine of required striding across (across). Along with expand improving, described heat recovery system is set to the exhaust temperature that reduces for greatly.

In another embodiment, purpose is temperature and the system effectiveness that promotes high energy (" the work ") fluid of described heat. In this class embodiment, three fluid VAST burners are operationally controlled the transverse temperature that enters decompressor and are distributed, and the preferred accurately flow of control that uses. This is so that can be in the control pollutant level, and obtains higher average fluid temperature (F.T.) under the identical condition of peak temperature. Preferred thermal technology's section (hot section) of using diluent (for example water and/or steam) to come (substituting the air cooling) cooling burner and decompressor. Preferably the diluent with heat enters described burner from upstream recirculation, thereby avoids the diluent cooling of described high energy (work) fluid, and further reduces compressor size and cost.

In another embodiment, another purpose is to reduce processing cost and the energy of the fluid that contains oxidant of input. In this class embodiment, preferably come the oxidant fluid filtration (spray filter) of spraying to input by direct contactor (contactor) with excessive diluent. The size of adjusting input sprayer and filter is used for lower oxidant stream. Can improve with cold diluent the density of input fluid.

In another embodiment, purpose is that the power that relatively produces reduces that the compression gaseous state contains the required power of oxidant fluid and equipment in the common ultra-poor burning, thereby increase the clean specific power of compressor and turbine (namely, the turbine general power deducts pumping power again divided by corresponding mass flow), and reduce system cost. In this class embodiment, preferably reduce the excessive gaseous state that is typically used as diluent with some vaporizable diluents at least and contain oxidant fluid, and pump merit with liquid pump and substitute air pump and pump. When every volume high-energy fluid flow through described decompressor, the diluent of vaporization can transmit more heat.

In another embodiment, the compressor in preferably circulating is set to the described fluid that contains oxidant is cooled off, and reclaims heat in the compression process with diluent simultaneously. The ground of instructing in the patent application preferably improves the spatial distribution that fluid is carried in compressor forecooler, intercooler and the intercooler (intra-cooler) with direct fluid contact device in described circulation as described ' 191. Can adopt the surface heat exchanger that uses cold diluent, and the diluent after being heated enters in heat-exchange system or the burner and re-uses.

In another embodiment of the present invention, purpose is that running is controlled at the level of major pollutants simultaneously and is lower than required boundary under near the condition of chemical dose. Preferably the VAST burner with the cross direction profiles that can control the fluid conveying operationally provides near the condition of chemical dose and the cross direction profiles of temperature, realizes simultaneously lower pollutant emission. In this class embodiment, by using the burner that can limit peak combustion temperatures, use simultaneously low excessive oxidant, be the discharging of nitrogen oxide (NOx) basically. Can operationally control the burner that transverse temperature distributes and the fluid component distributes by using, can realize good fuel oxidation, while carbon monoxide emission and residual propellant composition are less.

In another embodiment, purpose is that configuration can operate to provide one or more VAST circulation among hot water, saturated vapor and the superheated steam according to the concrete needs of using in cogeneration of heat and power (CHP). In this class embodiment, preferably can be at the described hot fluid of one or more position acquisitions and machinery or the electric energy of described heat and quality transmission system. Preferred diluent conveying, recuperation of heat and described burner are controlled, control so that flexibility carried out in the conveying of diluent (being steam), total amount of heat Q and machinery or the electric energy of vaporization.

Should be pointed out that some purpose of the invention described above embodiment and advantage are for to the present invention and be better than the purpose that the advantage of prior art describes and provide. Obviously, be to be understood that any specific embodiments of the present invention all there is no need to realize all these purposes or advantage. Therefore, for example, will be understood by those skilled in the art that can implement or put into practice the present invention realizes or increase one or more advantages teaching herein, and needn't realize other purpose or the advantage that this paper instructs or points out.

                     Brief description of drawings

By the general introduction to general aspects of the present invention and some feature and advantage, those skilled in the art can learn some preferred embodiment and modification thereof at an easy rate from the detailed description that this paper makes with reference to the following drawings, each has the feature and advantage corresponding to one embodiment of this invention in these accompanying drawings, wherein

Fig. 1 is the schematic diagram that the whole heat that adopts in the VAST circulation and quality are transmitted collocation method and possible configuration;

Fig. 2 is the schematic diagram with VAST water circulation (VAST-W) of intercooler, surface condenser, recompression machine and preheater;

Fig. 3 has the VAST water of intercooler, direct contact type condenser, recompression machine and preheater and the schematic diagram of steam circulation (VAST-WS or VASTEAM);

Fig. 4 is the schematic diagram with VAST backheat steam circulation (VAST-WSR) similar shown in Figure 3 of humidifier and regenerative apparatus;

Fig. 5 is the sectional drawing (break-out) with simple oxidant delivery system of single compressed machine;

Fig. 6 is the sectional drawing that has treating apparatus and choose the oxidant delivery system of the cooling stream of delivering to decompressor thermal technology section wantonly;

Fig. 7 has treating apparatus, a plurality of compressor assembly, and can carry to decompressor thermal technology section the sectional drawing of the oxidant delivery system of cooling stream;

Fig. 8 is detailed oxidant delivery system sectional drawing, and that wherein compressor formation (train) can have is pre-cooled, middle cooling or interior cooling and rear cooling device, and the cooling agent fluid is from compressor cooling agent system;

Fig. 9 is the schematic diagram of surface heat switching equipment;

Figure 10 is (heat rejection) the fluid cooling device schematic diagram with heat radiation;

Figure 11 is the rough schematic of liquid-gas contactor or direct contactor heat exchanger;

Figure 12 is the oxidant delivery system that adopts the compressor formation with diluent spraying preliminary treatment, diluent injection compressor and decompressor cooling;

Figure 13 has further shown to have the details that diluent injects the compressor formation of compressor;

Figure 14 is the schematic diagram with diluent induction system of simple diluent/cooling agent conveying;

Figure 15 is the schematic diagram of diluent with tape processing unit/cooling agent diluent induction system of carrying;

Figure 16 is the schematic diagram with fuel delivery system of simple fuel conveying;

Figure 17 is the schematic diagram with fuel delivery system of fuel conveying and treating apparatus;

Figure 18 is the sketch of heat generating component and cooling system thereof;

Figure 19 is the sketch of the optional heat-proof device of cooling system and surface heat exchanger;

Figure 20 is the sketch with decompressor of or whole two surface heat exchange systems, and this system has the coolant flow that uses diluent or directly contacts cooling device;

Figure 21 is the sketch with combustion system of fuel, oxidant fluid, liquid diluent and steam diluent induction system and burner cooling system;

Figure 22 is the schematic diagram by reclaiming and cooling off low temperature, middle gentle high temperature heat source with the diluent of heat;

Figure 23 has the schematic diagram that diluent injects the single decompressor expansion system that cools off;

Figure 24 is the schematic diagram with many decompressors expansion system of decompressor cooling system, and this decompressor cooling system adopts surface heat exchange and heat reclamation device;

Figure 25 can be expanded to the subatmospheric schematic diagram that diluent reclaimed and recompressed the expansion system of device that has;

Figure 26 is the schematic diagram with expansion system of the injection of inter-stage steam, diluent recovery and recompression and steam injection;

Figure 27 is the schematic diagram with the economizer (economizer) the liquid diluent of heat after expansion fluid is recycled to processing;

Figure 28 is the signal of reclaiming heat and can operationally warm water, hot water, steam and superheated steam be delivered to economizer, evaporimeter and the superheater of user's application and/or burner;

Figure 29 reclaims heat and can be operationally hot water and/or steam be delivered to that the user uses and/or the signal of economizer, evaporimeter and the superheater of burner;

Figure 30 is the schematic diagram of the part of the heat of component cooling system of compressor and quality transmission system;

Figure 31 is the schematic diagram with part of the heat of economizer, evaporimeter and decompressor component cooling system and quality transmission system;

Figure 32 uses regenerative apparatus, aftercooler, humidifier, economizer, evaporimeter and the heat of superheater and the schematic diagram of quality transmission system;

Figure 33 uses regenerative apparatus, aftercooler, humidifier, the heat of two economizers, evaporimeter and superheaters and the schematic diagram of quality transmission system;

Figure 34 is the schematic diagram of heat and quality transmission system, wherein reclaims diluent by the surface condensation device with cooling agent system;

Figure 35 is the schematic diagram of heat and quality transmission system, wherein reclaims diluent by direct contact type condenser and cooling agent system;

Figure 36 is the schematic diagram of heat and quality transmission system, wherein reclaims diluent by the surface condensation device with district heating in the cooling agent system;

Figure 37 is " wet " comparison diagram of capital cost of circulation of mounted VAST-W, VAST-WS and prior art;

Shown in Figure 38 is that the internal rate of return (IRR) (Rate of Return) of the circulatory system of VAST-W, VAST-WS and prior art is to the result of LHV cycle efficieny mapping;

Shown in Figure 39 be 50MW, 1300 ℃ the time, the result that the LHV cycle efficieny of VAST-W, VAST-WS, VAST-WSR and prior art circulation is mapped to the ratio of net power and compressor air flow (flow rate);

Shown in Figure 40 is that the LHV cycle efficieny of the circulation of VAST and prior art when 50MW and TIT=1300 ℃ is to the result of net power and the mapping of turbine flow ratio;

Shown in Figure 41 is that the unit net power discharge of VAST and prior art circulation when 50MW and TIT=1300 ℃ is to the result of water/intake air than mapping;

Shown in Figure 42 is that the ratio of the net power of circulation of VAST-W, the VAST-WS of 50MW and prior art and turbine flow velocity is to the result of air/fuel relative scale λ mapping;

Shown in Figure 43 is that the internal rate of return (IRR) of the circulation of VAST and prior art when 50MW and TIT=1300 ℃ is to the result of air/fuel relative scale λ mapping;

Shown in Figure 44 is that the ratio of the compressor supplementing water of the circulation of VAST and prior art when 50MW, TIT=1300 ℃ and 1.05 λ and fuel is to the result of pressure ratio β mapping;

Shown in Figure 45 is that the ratio of steam demand " Q " and net power of VAST and STIG circulation when 5MW and TIT=1000 ℃ is to the result of total amount of heat demand " Q " to the ratio mapping of net power;

Shown in Figure 46 is that the LHV coproduction efficient of VAST-W, VAST-WS and the circulation of STIG prior art when 5MW and TIT=1000 ℃ is to the result of total amount of heat demand " Q " with the ratio mapping of net power;

Decompressor pressure ratio and the result of each compressor pressure ratio to the mapping of air compressor pressure ratio for VAST steam circulation (VAST-WS) shown in Figure 47;

Shown in Figure 48 is the result that net power and turbine flow velocity ratio are mapped to water/air ratio;

Shown in Figure 49 is that the internal rate of return (IRR) % of different VAST circulations of disposing is to the result of LHV cycle efficieny mapping;

Shown in Figure 50 is that expansion ratio is to the result of recompression machine pressure ratio/compressor pressure ratio mapping;

Figure 51 is the flow chart of the collocation method of VAST-hydro-thermal mechanics loop structure;

Figure 52 is the flow chart of the collocation method of VAST-hydro-thermal mechanics loop structure;

Figure 53 is the schematic diagram of steam re-injection formula gas turbine (STIG) circulation prior art;

Figure 54 is the schematic diagram that intercooled recycled water injects (RWI) circulation prior art;

Figure 55 is the schematic diagram of intercooled humid air turbine  (HAT ) circulation prior art;

Figure 56 is the schematic diagram of intercooled humid air water re-injection formula turbine (Humid Air Water Injected Turbine, HAWIT) circulation prior art.

                     Detailed description of preferred embodiments

General introduction

The United States Patent (USP) 3 of Ginter, 651,641,5,617,719,5,743,080 and 6, instructed for 289, No. 666 mainly and circulated to cool off combustion process by liquid heat diluent (such as water) pumping is entered thermodynamics, reduced the VAST thermodynamics power cycle of the use of excess amount of diluent air. This VAST (" increment steam technology (Value Added Steam Technology) ") circulation is Brayton and mixing that Rankine circulates, and preferably uses fluid water as diluent. This recycles the high-energy fluid that forms in the VAST direct contact type fluid combustion device of the hot product that contains at the same time combustion process and superheated steam. This hot high-energy fluid preferably expands by decompressor and produces shaft power and/or electrical power. For example, by turbine or reciprocal plant equipment. This circulation also can provide cogeneration of heat and power (CHP).

With reference to Fig. 1, the recycling combustion system of VAST thermodynamics (Combustion System) 4000 forms high-energy fluid and is transported to expansion system (Expansion System) 5000, forms expansion fluid and output work output (Work Output). For example by turbine working fluid is expanded. Described expansion system is inflatable to subatmospheric pressure, and the expansion fluid of recompression cooling is put back to external environment side by side.

Utilize heat and quality transmission system (Heat and Mass Transfer System) 6000 to come around described system distribution diluent. This transmission system reclaims heat from for example expansion fluid, the assembly of cooling such as combustion system and expansion system, and the assembly that is heated (heated component) of cooling such as motor, pump, bearing and electromagnetic transducer and controller. It receives the merit input, for example to motor, pump and bearing. Be above-mentioned purpose, it can be to system or assembly, and for example described combustion system, expansion system and oxidant delivery system are carried the diluent of cooling diluent and acceptance heating. This heat and quality transmission system can use the fluid that contains diluent, the fluid that contains oxidant, the fluid that contains fuel or cooling agent fluid to receive back and forth heat. It can discharge the fluid of the cooling after the expansion. It can be provided for the heat or the cold fluid that heat or cool off. It also can discharge in diluent, water and the heat one or more.

The fuel that configuration fuel delivery system (Fuel Delivery System) 3000 will receive after fuel also will be processed is delivered to combustion system 4000 through described heat and quality transmission system 6000. This needs merit input to carry out the pump conveying and fluid is processed. Oxidant delivery system (Oxidant Delivery System) 1000 will contain oxidant fluid (being called " oxidant ") be delivered to combustion system 4000, heat and quality transmission system 6000 and expansion system 5000 one or more. It needs merit input to carry out fluid compression and/or pump is carried and fluid is processed. Diluent induction system (Diluent Delivery System) receives diluent outside and that reclaim, and the diluent after will processing is delivered to heat and quality transmission system 6000. It needs merit input to carry out the pump conveying and fluid is processed.

VAST circulation preferably is pumped into aqueous water, is delivered to the water of decompressor 5100 upstreams by direct contact, particularly with described compressor and decompressor between shown in burning fluid or high-energy fluid in the burner contact to produce steam. The steam with the highest possibility temperature that formation can be used in the turbine 5100 of cold blade like this. Described VAST system preferably uses low grade (insulted) pressure vessel that remains on relative low temperature, so that can use cheap pressure vessel material and structure. The method has been avoided conventional metallurgical restriction, and namely the combustion heat must be by the surface heat exchanger transmission. Therefore, it has avoided the main temperature limiting of conventional steam dynamical system, and corresponding temperature working fluid and the restriction of system effectiveness.

According to Carnot's theorem (Canot ' s law), along with the high temperature of the high energy (working fluid) of described decompressor entrance and the difference between the low temperature of the described decompressor outlet numerical value rising thermodynamic efficiency divided by higher absolute temperature raises. Compare the high pressure metallurgy of 1373K (1100 ℃) and learn restriction, use the gas turbine of VAST circulation and can under the temperature of about 1773K (1500 ℃), work. The preferred three fluid combustion devices that use the embodiment of instructing in the relevant three fluid patent applications of VAST circulation. This three fluid combustions device is so that the operator can very appropriate and accurately control or the peak temperature of the high-energy fluid F405 of restriction outflow burner, make it reach peak operation temperature desirable setting or that allow, this ideal or allowable temperature are to be determined by turbine blade material tolerable temperature and stress under the relevant blade cooling condition that provides. It is also so that can control the spatial temperature distribution that the described burner of outflow enters the high-energy fluid F405 of described decompressor.

By this accurate peak temperature control, under given existing blade cooling condition, the user controls to meet the required temperature of described turbine blade by conditioned space temperature and distributes, and increases the mean temperature of high-energy fluid F405 with this. Cool off burner bushing pipe (liner) with hot diluent, reduce or the alternative conventional hot diluent of gaseous state that is used for cooling off described bushing pipe. Then the diluent after will heating is conveyed into the described burner from the upstream. From described bushing pipe, thermal loss is looped back combustion chamber 4100 like this, avoided the mean temperature that the major part of high-energy fluid F405 is relevant in the prior art to reduce.

The embodiment of one or more in preferred these methods of use increases available average (the highest) temperature of high-energy fluid F405 and correspondingly increases the Kano thermal efficiency with respect to routine techniques, keeps simultaneously the peak temperature in decompressor 5100 downstreams constant. Identical peak value turbine inlet temperature (Turbine Inlet Temperatures, TIT) for example.

By preferred reduction or alternative excessive oxidant cooling stream commonly used by described bushing pipe, the user improves the Space Consistency through the static pressure distribution of the high-energy fluid F405 of burner outlet and speed distribution. These parameter distribution of raising high-energy fluid F405 have improved the type of flow in turbine 5100 substantially, and have improved this turbine efficiency.

The VAST circulation is preferably cooled off expansion fluid and the described diluent of condensation in decompressor downstream with direct heat exchanger 7500. Compare with the surface heat exchanger of routine techniques, by using distributed direct contacting with fluid condenser 7500, the user has improved the more approaching temperature that hot transmission causes. Effective flow area when it has improved by condenser 7500 has also reduced effective pressure drop and energy loss. Use one or both embodiments used simultaneously in these methods to reduce the effective low temperature in the Carnot efficiency, thereby improve Carnot efficiency.

By carrying liquid heat diluent (such as water) to substitute the most excessive oxidant fluid (such as air) that contains, some embodiment has obviously reduced parasitism (parasitic) pumping loss in oxidant fluid compressor 1300 and the hot diluent pump. Use and spray the pressure loss that direct contact type filter (spray direct contact filter) reduces described parasitic input fluid. This class filter has reduced the Efficiency Decreasing that dust causes in compressor 1300 interior accumulations. These direct contact type filtering and cleaning devices have reduced the amount in the fluid that carries the condensation behind the turbine. This has reduced the parasitic pumping that recycles the required filtration of this condensation fluid, pH balance and correspondence. By reducing one or more these parasitic pumping loss, various embodiments described herein have obviously improved system's net efficiency.

By using one or more of three fluid combustion devices, direct contact type condenser 7500 and the direct contact type filter described in as herein described and ' 191 patent application and the three fluid patent applications, can substantially improve clean specific power and the efficient of the circulation of VAST thermodynamics.

Heat and quality exchange system

Economizer (economizer)

With reference to Fig. 2, in some configuration, the user preferably provides heat exchanger economizer (ECO) 6500 to heat hot diluent F249 from diluent recovery system 6010 (for example by condenser or preheater 7100), and before the expansion fluid F420 that discharges from decompressor (EXP) 5100 arrives described condenser or preheater from wherein reclaim heat (referring to, for example figure 02, figure 03, figure 04 and Figure 27). In the VAST circulation, the expansion fluid F420 that leaves decompressor 5100 is normally undersaturated. Therefore can use surface exchanger to economizer 6500.

In some configuration, the user preferably only allows the hot diluent of recovery of part pass through described economizer 6500. For example, with further reference to Fig. 2, it provides current divider 6320 that logistics F220 is split into the logistics F248 part that flows to economizer 6500 and the diluent flow F250 part that flows to oxidant delivery system 1000. This current divider 6320 is so that can initiatively control fluid ratio between logistics F248 and the logistics F250. It preferably is delivered to the diluent of some or all balance needs the system of cryogen part, and cool off such as expansion fluid or contain liquid stream and/or the heat-producing device of oxidant fluid, thus control appliance temperature and/or raise the efficiency. For example, the user who instructs such as ' 191 patent application preferably guides to the part cold flow direct contact type blender diluent is spurted into the first compressor 1310.

Similarly, instruct such as ' 191 patent application, the user can provide the injection intercooler of one or more direct contactors between at different levels as one or more low pressure compressors 1310 and high pressure compressor 1350 or compressor. Instruct such as three fluid patent applications, they can provide diluent to cool off the pressure vessel of the combustion chamber 4100 in the burner 4000 similarly. In the circulation of the VAST-WS shown in Figure 37 and the table 1 configuration result, make the diluent economizer 6500 of partly flowing through directly enter burner 4000 with part and compare with all hot diluents are heated by described economizer, have better thermoeconomics benefit.

The relative circulation capital cost $ of the power cycle of table 1 use fluid water/kW@50MW, TIT=1300EC, Beta=30
								Circulation	Associating	STIG	RWI	HAWIT	HAT	VAST-W	VAST-WS
Compressor	138.7	107.9	112.0	100.8	100.1	89.3	79.2
								Burner	1.6	1.5	1.4	1.1	1.1	0.8	0.9
Gas expander	50.3	51.4	47.7	45.1	43.9	45.8	42.1
								Regenerative apparatus			4.3	4.2	4.4
Saturator				4.3	4.5
								Superheater	10.3	6.0					3.1
Evaporimeter	32.2	9.5					6.3
								Economizer	11.4	8.3	3.8	12.3	26.7	14.9	9.8
The steam expansion machine*	75.8			5.5		4.6	11.0
								Generator	37.8	36.5	36.5	36.6	36.6	36.7	36.6
Pump ﹠ auxiliary equipment	1.9	0.7	1.1	2.0	1.9	3.3	1.8
								Install etc.	327.6	201.8	188.2	192.9	199.6	177.8	173.5
Total $/kW	687.6	423.6	395.1	404.9	418.9	373.2	364.1
								*﹠ condenser, or condenser ﹠ recompression machine; Cost equation is according to Traverso 2003

In the configuration of revising, the user preferably provides variable current divider 6320 afterwards in diluent recovery system 6010 (for example surface condenser 7400), part or all of hot diluent is transported to downstream preheater 7100, to reclaim heat from the expansion fluid F421 that is disposed to diffuser (Diffuser) 5900 (or exhaust apparatus or chimney), this diffuser 5900 is used for expansion fluid F475 is disposed to external environment. This current divider 6320 allows to regulate the amount by the hot diluent flow of preheater 7100, thereby directly affects the temperature of the hot diluent flow F270 that flows out described preheater. This also affects the amount of the diluent flow F249 of the described economizer of flowing through, thereby the temperature of the hot diluent flow F275 of economizer 6500 is flowed out in impact.

In some configuration, the user is the described Conversion of Energy of operation system under " circulation of VAST water economizer " (VAST-W) goes up with the condition of economizer preferably. They preferably are pressurized to enough pressure with hot diluent (such as water), the diluent F275 after the heating in economizer 6500 downstreams is transported to combustion system 4000 and does not evaporate. For example they can come the current F249 that diluent water flows after F248 pressurizes and will pressurize is transported to economizer 6500 with pump 7800, and then form and the hot water stream F275 that carries pressurization to combustion system 4000, and water can not flash to steam before being delivered to described burner. Compare with regular circulation, decompressor 5100 is used high expansion ratio and cools off expansion fluid F420, the described decompressor of per unit mass flow (turbine) can produce larger power. Compare with correlation technique, leave the expansion fluid F420 that described decompressor enters economizer 6500 and have lower turbine-exit temperature (Turbine Exit Temperature).

Utilize the circulation of VAST economizer, by using suitable burner and the configuration oxidant delivery system relevant with described decompressor, do not cause surging (surge) etc. to hold the hot diluent that is delivered to burner, preferably operate near stoichiometric condition. Shown in Figure 37 and table 1, compare with the configuration of correlation technique, can use less substantially more cheap compressor by this VAST-W configuration user. Similarly, and unite circulation (Combined Cycle), STIG, HAWIT and HAT recycle ratio shown in the table 1, the less cost of area of the economizer that uses separately in the VAST-W circulation is lower.

Such as Figure 37 and the relative installation capital investment digital proof shown in the table 1, (STIG or suitable CHENG circulation-Figure 53), recycled water inject (RWI-Figure 54), humid air turbine (Humidified Air Turbine with uniting circulation (CC), steam re-injection formula gas turbine^，HAT ^Or suitable steam turbine (EvGT) circulation-Figure 55), and humid air water " wetting " of injecting the prior art of turbine (HAWIT-Figure 56) " wet " circulation circulate and compare, the VAST-W system has advantage economically. Figure 37 and table 1 are assumed to the power system of 50MW, and it has 1300 ℃ of common turbine inlet temperatures, and the compressor pressure ratio during work is 30 (the burner inlet pressure of about 30 bar). Be 4000 or 8000 hours a man-hour in hypothesis year simultaneously, and heat is used for such as district heating or steam, does not benefit from extra recovery. These recycle ratios in, according to Traverso ﹠ Massardo (2003) and be similar to Traverso ﹠ Massardo (2002), each is recycled identical assembly cost equation and ratio is installed hypothesis (proportional installation assumption). Also suppose simultaneously the U.S.'s average natural gas of industry in 2000 and electricity rates (referring to table 2).

Table 2 thermoeconomics suppositive scenario
		Inflation	2.5％
The nominal growth rate (Nominal Escalation Rate) of the equipment cost of buying	2.5％
		The nominal growth rate of fuel cost	3.0％
Build the beginning time (January)	2001
		Building time	2 years
The economic life of factory (predicted life)	20 years
		Taxing purpose (tax purpose) factory's life-span	10 years
Debt-financing part	50％
		Preference stocks-financing part	15％
Common capital stock-financing part	35％
		Year return of debt-needs	5.5％
Year return of preference stocks-needs	6％
		Year return of common capital stock-needs	6.5％
Average income tax rate	30％
		Fuel price (natural gas)	4.0E-6$/kJ
Go the price of mineral water	0.5$/m 3
		The electricity price	1.32E-5$/kJ
Be equivalent to number in year man-hour	8000h
		The operation and maintenance cost	4% of FCI

With reference to Figure 38, compare with the wet circulation of routine, the user can obtain higher thermoeconomics benefit by the VAST-W circulation with competitive efficient. Among Figure 38, the scale on figure right side refers to 8000 hours/year basic load operation. The left side refers to that the fractional load of estimating 4000 hours/year operates i.e. 50% load. By these configurations, user's contestable ground adopts and to be higher than 15, preferably is higher than 30, more preferably is higher than 40 pressure ratio β and moves the VAST-W circulation. In the VAST-W that estimates circulation configuration, shown in the pressure ratio β scope, in the pressure ratio β scope of preferred 20-30, internal rate of return (IRR) % (Internal Rate of Return) is higher than substantially relevant " wet " and circulates. Low heat value (LHV) cycle efficieny of the VAST-W circulation that shows has competitiveness to STIG and the HAWIT circulation that demonstrates immediate economic benefit.

Further with reference to Figure 38, to the U.S. average industrial fuel and the electricity rates in 2000 of supposing, under all were higher than about 15 pressure ratio, the internal rate of return (IRR) of VAST-W circulation was higher than the STIG circulation. Estimate, further improve and the water discharge pressure that reduces by 165 bar of supposition in the VAST-W configuration can further improve these benefits. It should be noted that with this power particularly the lower two press water laterals of fractional load operation close circulation and dispose and compare, VAST-W disposes has better income. The circulation configuration of uniting that efficient is higher is adjusted to obtain the highest efficient, and the higher circulation configuration of uniting adjusts to obtain the highest life cycle economic well-being of workers and staff to the low IRR of efficient. To shown in VAST-W and other loop adjustment, than under to obtain the highest efficient at setting pressure. Improved configuration can further improve the income of these circulations.

Evaporimeter (boiler)

VAST steam circulation (VAST-WS)

With reference to Fig. 3 (relevant with Fig. 2), in certain embodiments, the user preferably adopts heat exchanger when reclaiming heat from expansion fluid diluent to be boiled the formation steam diluent. Some heat exchanger that can be used for boiling diluent can be configured to especially independently that evaporimeter (EVA) 6600 comes heat of evaporation diluent F251, reclaims used heat from the expansion fluid F420 that flows out decompressor 5100 simultaneously. Evaporimeter 6600 is positioned at the upstream of economizer 6500, relates to the high-energy fluid (or be positioned at the downstream, relate to the diluent fluid F250 that leaves described economizer) of the expansion of flowing out decompressor.

With further reference to Fig. 3, the configurable heat exchanger of user provides independently superheater (SH) 6700, so that the diluent steam F252 that forms in the evaporimeter 6600 is overheated and formation superheated steam F275. This superheater 6700 is preferably placed at the upstream of evaporimeter 6600, and is relevant with the high-energy fluid stream F420 of the expansion of leaving decompressor 5100. In this configuration, overheated steam diluent F275, saturated steam diluent F252 and the hot liquid diluent F251 of generation the process that reclaims heat from expansion fluid F420. These diluent flows preferably are delivered to burner and/or are used for other heat and use. For example, with reference to Fig. 3, the user preferably disposes VAST steam circulation (VAST-S) by boil diluent (such as water) when the expansion fluid F420 in turbine 5100 downstreams reclaims heat, thereby forms hot water F251, saturated vapor F252 and any two or more among the overheated steam F275. With reference to Figure 44, in some configuration, the pressure ratio β of user's capable of regulating compressor adjusts liquid diluent to the ratio of the vaporization diluent of formation with this.

In some configuration, the user preferably only carries the hot diluent of part economizer 6500 heating by evaporimeter 6600. With further reference to Fig. 3, the user preferably offers described burner with liquid diluent as the hot diluent of part. They preferably provide the heat of vaporization diluent of a part to described burner. The thermoeconomics of recuperation of heat and the efficient of system have been improved like this.

With reference to Figure 29, in improved configuration, user's variable current divider 6350 of preferred configuration between economizer (ECO) 6500 and evaporimeter (EVA) 6600 is controlled diluent flow, the diluent that is delivered to evaporimeter with control and ratio to the diluent of other position. For example, the user preferably controls from economizer 6500 to combustion system 4000 diluent and ratio to the diluent of evaporimeter 6600 with current divider 6350. Like this, can regulate the amount of the hot diluent of this evaporimeter of flowing through, thus the quantity of steam that regulate to form and the temperature of diluent that flows out the heat of this economizer. The user preferably controls this ratio and leaves the temperature of fluid of this economizer with control than the lower slightly several years of boiling point. For example, suppose that the fluid temperature (F.T.) of the heat of leaving economizer and the temperature difference between the boiling point are 3 ℃. These remote-effects leave the temperature of the expansion fluid F420 of economizer.

Superheater (gas-gas-heat exchanger)

In improved embodiment, the user preferably disposes the heat exchanger that can form overheated diluent when reclaiming heat from the expansion fluid that leaves decompressor 5100. For example, with reference to Fig. 3, the user can add superheater (SH) 6700 in the upstream of economizer 6600 (with evaporimeter 6500) and heat the hot diluent steam F252 of vaporization, reclaims simultaneously the heat of higher temperature from the high-energy fluid F420 that leaves decompressor 5100. VAST steam circulation (VAST-WS) preferably includes evaporimeter (EV) 6600 and superheater (SH) 6500.

Arrive the diluent of the heat of user's application

With reference to Figure 29, in some configuration, preferably the heat recovery system that adopts among the VAST-WS shown in Figure 3 is improved, between evaporimeter 6600 and superheater 6700, to comprise variable current divider 6360. Like this can distribution portion or whole diluent vapor stream F252 (for example saturated vapor) carry out heat and use (for example heating or cooling), and make remaining vaporization diluent flow flow to superheater 6700. Current divider 6360 can be regulated the steam flow through hot device 6700. The user can utilize this current divider control from the temperature of the overheated hot diluent of this superheater outflow.

With reference to Figure 28, be other inside or outside heat application, can improve VAST-S shown in Figure 3 circulation by adding one or more flow dividers, with one or more in heat and the warm diluent of quality transmission system 6000 supplies, warm diluent, saturated vapor and/or the superheated steam arbitrarily or optionally. For example can between diluent treatment system (DTS) 2010 and economizer (ECO) 6500, dispose flow divider 6310, to use convey warm to warm water; Can between economizer (ECO) 6500 and evaporimeter (EVA) 6600, dispose flow divider 6340, to use the hot diluent fluid stream of transport portion to hot water; Can between evaporimeter (EVA) 6600 and superheater (SH) 6700, dispose flow divider 6360, to use the diluent of carrying vaporization to steam; Can between superheater (SH) 6700 and combustion system 4000, dispose flow divider 6370, carry overheated diluent to use to superheated steam.

With reference to Fig. 1, the assembly or the heat generating component that preferably in energy conversion system, are heated according to required cooling with one or more these diluent flows. For example, cool off described burner and described decompressor one of them or both simultaneously. With reference to Figure 28, similarly, can outside described energy conversion system, one or more these fluids be used for the application of other warm water, hot water, saturated vapor or supersaturated vapor.

With further reference to Figure 28, for the diluent flow of the heat that provides is provided to the user in control in the described combustion process of control, the user is configuration flow divider 6320 before the heat exchanger of the fluid of needs heat preferably, so that the lower diluent flow of temperature is controlled combustion process to described burner, still reclaim enough heat so that the user to be provided required hot-fluid simultaneously. When also needing hot water, can with this flow divider 6320 or similarly flow divider be positioned over again downstream (relatively described expansion fluid) more near the position of the cooling segment of diluent recovery system (DRS) 6010. As shown in Figure 28, can merge with blender 6190 the liquid diluent stream of different temperatures, and send into together described burner. Also can according to the control of required thermal gradient, also these diluent flows can be sent into described burner with the form of multiply logistics.

These class control measure so that the user can utilize the heat that can from described expansion fluid, reclaim partly or entirely. Regulate the diluent flow that enters burner according to the temperature difference of diluent. According to user's heat supply, the user preferably with its with can operate to be in harmonious proportion awfully hot VAST burner to cold diluent temperature and be combined with.

Pressure or temperature or both simultaneously requirements when downstream user (for example district heating) needs or requirement is lower can reduce at least one parameter in pressure or the temperature with one or more attemperators that contain or do not contain attemperator. Can be used as the source of insulation water in the circulation with the hot diluent (fluid that for example returns from district heating) of external source.

Regenerative apparatus (gas-gas-heat exchanger)

With reference to Fig. 4, the user can improve VAST-WS circulation (for example shown in Figure 3) by adding regenerative apparatus (REC) 6800, heat is recovered to the oxygen-bearing fluid that offers burner 4000 from expansion fluid. This improvement further shown in figure 32. For example, can provide current divider 6410 that the expansion fluid of heat is divided into two strands. One hot expansion fluid F422 one or more heat exchangers of flowing through, make recuperation of heat to diluent with evaporation and the overheated fluid (for example one or more superheaters and evaporimeter shown in Figure 4) that contains diluent. The expansion fluid of another burst heat regenerative apparatus (REC) 6800 of flowing through, with heating from the input of oxidant delivery system (such as compressor 1350) contain oxidant fluid F160, the oxidant fluid F435 that contains after will heating afterwards is delivered to burner 4000.

With further reference to Fig. 4, can be in blender 6180 will merge from the expansion fluid of two bursts of coolings of regenerative apparatus 6800 and evaporimeter 6600, and the economizer 6500 of flowing through, hot further from the fluid that the part of described merging is cooled off, to reclaim, and heating contains the fluid (for example hot water) of diluent. Economizer 6500 reclaims heat and heats the fluid that contains diluent from the expansion fluid that reconsolidates. Preferably make diluent flow after the heating of leaving economizer through current divider 6350, between evaporimeter 6600 and other are used, to distribute diluent flow.

The diluent flow that is turned to by current divider 6350 preferably passes through another current divider 6351, so that the part diluent flow mixes with the oxidant fluid that contains of regenerative apparatus 6800 upstreams. Shown in the present embodiment, be transported to burner 4000 through another part diluent flow behind the current divider 6351.

With further reference to Fig. 4 and Figure 33, this liquid state contains the diluent fluid and also can be used for the diluent fluid that contains that oxidant fluid carries out rearmounted cooling (after-cool) that contains that leaves final compression section is mixed with other, and makes the diluent fluid that contains of this merging enter humidifier or " saturator ". This humidifier or saturator can be the packed layer contactors. The user preferably disposes the oxidant fluid that contains that direct contactor is distributed into the vaporizable diluent compression. For example water is sprayed by fairshaped direct contactor. Can reduce like this pressure drop of required volume and the described humidifier of process.

With reference to Figure 33, in the improvement project of the embodiment that above-mentioned back-heating type VAST circulates, can come to reclaim heat from second expansion fluid in regenerative apparatus 6800 downstreams with the second economizer 6510, and heating be delivered to the liquid diluent of humidifier or saturator.

In certain embodiments, the user disposes direct contactor hot diluent is conveyed into the containing in the oxidant fluid of compression of input regenerative apparatus, to help reclaiming heat from the expansion fluid in described turbo-expander downstream. The user preferably is conveyed into liquid diluent in the fluid of compression, increasing the specific heat of described compressed fluid, thereby improves the surface heat transmission, and reduces size and the cost of described regenerative apparatus.

Preheater

In certain embodiments, the user can utilize preheater 7100 with hot diluent (for example water) from low-temperature prewarming to suitable temperature, and before the expansion fluid (or " flue gas ") of the cooling that will be heated by recompression machine 5300 is discharged into environmental condition, from wherein reclaiming heat. (referring to, for example figure 02, figure 03 and figure 04). In some configuration, the effect possibility less of preheater, and the user can make up VAST-W, VAST-WS and the VAST-WSR circulation that does not contain preheater.

In improved configuration, the user preferably makes a part in the diluent of recovery by preheater 7100. They preferably are delivered to the system's part that requires or need cryogen with the hot diluent of recovery of some or all balances, come cooling fluid or equipment and raise the efficiency. (referring to, for example figure 02, figure 03 and figure 04 wherein make the F270 of described fluid partly flow to oxidant delivery system to cool off the oxidant stream of described compression).

For example, the user preferably makes the part cooling fluid flow to spraying feeding device (spray entrainer) and enters described compressor, or the spraying intercooler between low pressure and the high pressure compressor and/or cooling pressure container. In some configuration, heat through preheater with making whole hot diluents, make segment fluid flow produce higher thermoeconomics benefit through preheater. Therefore, the user preferably provides Low Temperature Thermal diluent F248 to economizer 6500, and without F270 described compressor is carried out the centre cooling, thereby improves cycle efficieny.

In other configuration, the user preferably substitutes the described regenerative apparatus in heating or the dynamical system with economizer in some configuration. Preferably include the recompression machine in these configurations. One of these measures or both can significantly reduce the temperature of the expansion fluid that leaves described decompressor. These measures have reduced operating temperature and the relevant cost of described heat recovery equipment very significantly. In some configuration, the user preferably includes evaporimeter and superheater.

One or more these measures have obviously improved the thermodynamic efficiency of heat supply and electricity generation system. For example, in the small-sized turbine of routine, often be equipped with regenerative apparatus is promoted to the system effectiveness under the about 100kW power of about 80kW-the backheating type small size turbine by about 23% of simple cycle about 30-31%. The associating efficient of supposing generator, power conversion apparatus and bearing is 80%, and then the VAST circulation can be increased to efficient about 3% or about 10% to about 33%.

Similarly, by improved power electronics, described VAST-W economizer and the circulation of VAST-WS steam make the efficient of system improve about 3-4%, or make efficient improve about 10%. The efficient of its hypothesis generator is about 98%, and it is about 95% that the frequency-converter power conversion electron is learned efficient, and the efficient of bearing and other assembly is about 93%-95%. For example, in these situations, can obtain the efficient (LHV) of about 32.5%-35.7% to the VAST economizer of about 100kW and the circulation of VAST steam.

Turbine inlet temperature significantly raises under these efficient. For example, to the small-sized turbine system of VAST of 100 kW that only have economizer, estimate that the efficient at 950 ℃ is about 32.5%, and efficient raises and raises along with turbine inlet temperature, being about 33.8% at 1000 ℃, is about 36.1% at 1200 ℃, is about 36.9% at 1200 ℃.

Similarly, the configuration of these recuperation of heat methods has reduced the cost of thermodynamic system. For example, in small-sized turbine system, for example about 200kW or less in, the cost of described independent regenerative apparatus usually approximates or is higher than compressor and turbine combination. In addition, the high temperature regenerative apparatus has taken most R and M expense (it is reported, be about 80%) in some system. By substituting described regenerative apparatus with evaporimeter, adopt higher pressure and expansion, the user make small-sized turbine dynamical system cost about 20-25%.

This combination of raising the efficiency and reducing cost has obviously improved the capital cost that and a plurality of following condenser whenever is provided and realizes corresponding parameter and benefit.

The fluid F460 of the cooling of expanding preferably crosses condenser with cold hot diluent reverse flow. The liquid state that contains the diluent fluid and be used for cooling that can reclaim condensation contains the diluent fluid, and come self cooled expansion fluid condensation contain the diluent fluid.

With reference to Figure 34, preferably select the surface heat exchanger 7400 of adverse current configuration. Obtain so lower the having a few of condensate flow temperature and pressure, obtained simultaneously higher recovery cooling agent and diluent temperature. Except described diluent is carried out the condensation, preferably this surface heat exchanger is set to reclaim some heats from the expansion fluid of described input. Therefore, the part heat is recycled in the coolant flow. The preferred diluent that uses is as described coolant flow. For example, high purity water. In improved embodiment, the user can provide cross-flow or and banish and put.

The low pressure of the cooling fluid of the expansion of diluent from condenser of condensation is pumped to required returning pressure. Can add barometric leg, and the bottom that pump is placed on described leg is to reduce or to avoid cavitation.

The hottest part from the condensate of described condenser preferably is recycled to heat and quality transmission system, and its flow approximates the amount that contains the diluent fluid of the conveying of decompressor outlet upstream, and is sent to various users' heat from heat exchanger and uses. These warm diluents are sent back to after treatment to compressor 1300, burner 4000 and decompressor 5100, again reclaim heat by one or more heat exchangers according to required. Collect enough warm diluent or cooling agent fluid from the coldest part of surface heat exchanger 7400, and loop circulation around described cooling.

In certain embodiments, burn with oxygen or oxygen-enriched air and eliminated part or almost all nitrogen and the hot diluent of other incompressible gaseous state. Similarly, reduce in certain embodiments or remove airborne nitrogen or other diluent and reduced energy, equipment and cost that from the expansion fluid of cooling, isolating the carbon dioxide that burning forms.

With reference to Figure 35, the user preferably uses distributed direct contact condenser 7500 in certain embodiments. Reduced like this near the time the temperature difference between expansion fluid and the cooling agent, and described expansion fluid is cooled to lower temperature. Compare with using conventional heat exchanger, these two kinds of measures all can improve the thermal efficiency of described power cycle. Estimate, use the direct contact type condenser can reduce the cost that diluent reclaims, thereby improve the thermoeconomics of described power cycle.

Instruct in the patent application of ' 191 especially with reference to Figure 83, as described, the user more preferably forms described direct contact type condenser with direct contactor. This has reduced the pressure drop by the expansion fluid of described condenser. The vertical countercurrent configuration of ' 191 patent application shown in Figure 83 can also be reclaimed the diluent of heat, and the temperature of this diluent reaches as high as the saturation temperature of the expansion fluid stream of input.

These cooling means condensations described expansion with the cooling high-energy fluid in most of steam and water vapour. This makes oxygen and the water vapour of residual nitrogen and carbon dioxide and small part in the expansion fluid of described condensation. Right, by the aflame nearly all excess air of basic removal, subsequently condensation and remove to form with the water that injects, these embodiments can make the gas concentration lwevel in the cooling discharging gas be the highest in all routine techniques that do not burn with oxygen-enriched air or oxygen (referring to, table 3 for example).

The oxygen of table 3 remnants and carbon dioxide vs intake air
					Intake air	Concentration-the drying of incompressible residual gas of discharging
The % stoichiometry	O2	CO2	O2	CO2
					mol％(vol％)	mol％	mol％	mol％
	334％	15.00％	4.26％	16.39％					6.40％
300％					14.31％	4.74％	15.61％	7.11％
	250％	12.94％	5.70％	14.07％					8.52％
200％					10.87％	7.15％	11.75％	10.64％
	150％	7.34％	9.63％	7.87％					14.20％
110％					2.04％	13.34％	2.16％	19.42％
	105％	1.07％	14.02％	1.13％					20.36％
100％					0％	14.77％	0％	21.40％

For example, be that the 110% stoichiometric oxidant fluid (for example oxygen in the compressed air) that contains makes diesel fuel burning with oxidant, gained carbon dioxide (CO2) accounts for about 13.34% volume ratio (or 19.42% mass ratio of Incompressible gas in the expansion fluid of described condensation, get rid of the butt of water vapour, suppose that Diesel#2 can be represented by C12H26-). On the other sidely be, input air with 334% chemical dose carries out the fuel-sean burning, the content of carbon dioxide is 4.26% volume ratio (6.40% mass ratio), wherein calculates 15% volume ratio (about 16.39% mass ratio) that oxygen accounts for remaining Incompressible gas with butt.

In certain embodiments, the user compresses subsequently and separates remaining carbon dioxide. Compare with conventional method, the gas concentration lwevel in the expansion fluid of described cooling is higher, has obviously reduced energy consumption and the cost of isolating described carbon dioxide. For example, at about 110% stoichiometric combustion synthesis in air Diesel#2, the mass percent concentration of the carbon monoxide that the user obtains is for using 303% of 334% stoichiometric air burning gained concentration by conventional fuel-sean burning system. Thereby when reclaiming the carbon dioxide of this high concentration, the used pumping power of user reduces by 67% approximately.

Preferably with filtering and adsorption method is removed alloy in the expansion fluid of cooling. Some embodiment adopts compression to separate with condensation and reclaims carbon dioxide. Other embodiment adopts pressure-variable adsorption or vacuum pressure-variable adsorption, and sorbing material and the method that carbon dioxide is preferably disposed used in these absorption. Some uses the chemisorbed method of using amine or other sorbing material that adopts. Other embodiment reclaims carbon dioxide with physics, electrochemistry or conducting membrane separation method.

Hot water-district heating

Except shaft power and/or electric power, in certain embodiments, the preferred configuration device of user provides hot diluent, hot diluent steam and/or the overheated hot diluent steam of heat. With reference to Figure 28, can in economizer and/or by the steam generation system, produce for example hot water and/or low or high steam. Similarly with reference to Figure 34, in surface condenser, in containing the process of diluent fluid from the liquid state of expansion fluid, condensation can produce hot water. But its delivering hot water or " district heating " are used. For example, plan to provide and return at 40 ℃ at 80 ℃. Similarly, as shown in Figure 35 and Figure 36, can reclaim temperature or hot water by the direct contact type condenser. Before described logistics being sent to one or more economizers, oxidant delivery system and district heating or other heat application, the user can select surface or direct contact type condenser according to the required degree from high-energy fluid recovery heat.

With reference to Figure 28, the user preferably disposes and/or controls the ratio of the hot diluent that flows to one or more in surface condenser, preheater, economizer, evaporimeter and/or the superheater or pass through from its bypass, with as required or heat is used or the particular requirement of cooling stream is regulated described flowing and temperature. With reference to Figure 45 (also referring to Figure 46), by this class measure, the user can adjust low-temperature heat quantity " Q " to the ratio of net power and the steam ratio to net power on a large scale.

With further reference to Figure 45, to identical steam hot-fluid Q steam, compare the circulation of VAST steam with the STIG circulation of prior art the ratio of the higher total heat Q of cardinal principle to net power is provided. For example, when being about 0-1.0 for steam/power ratio, compare for about 0.6-0.4 with the STIG circulation, heat/power ratio of VAST is about 1.1-1.3. These results are simulated being operated in approximately on 1000 ℃ the industrial steam turbine of 5MW. At this moment, simulation STIG circulates to produce the steam of maximum possible, correspondingly adjusts the maximum stream flow of compressor. Suppose that VAST steam circulates in relative air/fuel ratio λ and moves under 1.05 the condition. These higher heat/power ratio demand that obviously more approaching major part is commercial and light industry is used.

When needs or when requiring district heating, the user according to the quantity of steam of needs simultaneously can select VAST water or VAST steam circulate both one of. In some configuration, the user preferably disposes one or more in preheater and the economizer, and/or make relevant stream be delivered to adjusting by these assemblies the temperature of hot water of district heating and amount (referring to, for example Figure 28, Figure 36 and/or Figure 45).

In the district heating of using hot water is used, preferably return described energy conversion system after the described hot water cooling. Usually, water is partly lost in return loss in district heating system. In certain embodiments, the user reclaims excessive water also with its supplementing water as district heating from expansion fluid. This has been avoided providing the cost of supplementing water. In some improved embodiment, can come from the fluid that returns, to reclaim remaining heat with regenerative heat exchanger, the heating of diluent provides heat thereby reclaim heat and for example circulate to described VAST.

The steam that is used for other application

When needs or when requiring low-pressure steam, the user preferably uses the circulation of VAST steam. Circulate by VAST steam, in certain embodiments, the user preferably disposes one or more in preheater, economizer and the evaporimeter, and/or in these assemblies relevant stream with adjusting be heated the low-pressure steam produced quantity and temperature and/or be delivered to the quantity of the hot water of district heating. (referring to, for example Figure 28 and Figure 45).

Refrigeration plant

When needs or when requiring high steam, the user preferably uses the circulation of VAST steam. Circulate by VAST steam, the user preferably disposes one or more in preheater 7100, economizer 6500 and evaporimeter 6600 and the superheater 6700, and/or the relevant logistics by these assemblies, with as required or configuration amount and the temperature of regulating the high steam of conveying. In some configuration, they also are configured with as required or require to provide hot water and/or low-pressure steam system. (referring to, for example Figure 28 and Figure 45).

In some configuration, the user has disposed refrigerating system. For example cold water tank, ice storage device and/or cold stone storage facilities. The user preferably moves described freezing equipment at off peak periods and cools off the cooling agent fluid, and cools off described refrigerating system with it. For example, cold water, cold air or cold-producing medium.

When very large to the demand fluctuation of refrigeration service and/or mechanical energy and electric energy, the user transforms VAST circulation configuration and is preferably provided with the device that extracts and carry as required the refrigeration service from refrigerating system. In some configuration, the user preferably uses the oxidant fluid that contains of described refrigerating system cooling input. This help to improve the density of input air and the capacity of compressor, especially on date of sweltering heat.

Power improves

The user preferably provides diluent to cool off high-energy fluid in combustion process and/or the described combustor before decompressor. In this way, they have improved the amount of combustible fuel and oxidant, and the power capacity of system. So in the operating process, preferably keep the temperature of described high energy gas.

Burn systematic comparison with the use excess air of the prior art of routine as the fuel-sean of hot diluent, VAST circulates in to change or put forward high-power ability when keeping temperature has special advantage. In those systems, the extra fuel that burns has improved the temperature when high energy gas leaves burner, thereby has increased the breakdown speed to turbine blade and other thermal technology's section assembly. By the VAST circulation, the user preferably is independent of fuel flow rate and power level is controlled described temperature.

Under certain conditions, the user preferably improves the temperature of the high-energy fluid of burner outlet, to increase generating capacity and/or the turbine efficiency of turbine. For example, under the condition of urgent electricity consumption. By the improved temperature control method described in `191 patent application and the described three fluid patent applications, the time span that the preferred accurately described outlet temperature of control of user and this class temperature rise. The aging speed of turbine blade is carefully monitored these parameters relatively.

In some configuration, under the condition of the flexibility that given VAST circulates, the user preferably regulates cooling logistics and cooling agent, vapor (steam) temperature and/or the water coolant logistics that is delivered to turbine blade, improves the cooling of blade when rising with the temperature at described high-energy fluid. Compare with conventional correlation technique, this cooling to turbine blade is better, has reduced the breakdown speed of high-temperature operation. Thereby, reduce the frequency that blade is changed, and improved the lifetime of system cycle cost.

Flow and control

In some configuration, the flow that the user preferably provides driver and controller to regulate preheater, economizer, evaporimeter, flow divider, thereby as required or require to regulate these logistics. The user preferably disposes dynamic driver, controller and sensor, come the needs used according to the time or change in process etc. dynamically to control the relevant portion of hot water, low-pressure steam, high steam and power, for example these can make electricity consumption, waterpower, wind-force or thermo-mechanical drive.

In certain embodiments, the user disposes the hot diluent flow of multiply circulation and is heated to various temperature by reclaim heat from expansion fluid. For example, the user preferably provides cold water to come the cooling liquid state fuel delivery system to stop coking. As a supplement, the user provides hot water and/or steam to distribute with the temperature of controlling combustion process to burner, discharges thereby suppress NOx in the most of carbon monoxide of oxidation and other combustible component, and reaches required turbine inlet temperature. The user preferably carries tiny hot water to drip and/or steam, to help the restriction of expansion combustion stability. The user preferably carries liquid diluent, thus most of vaporization after the burning beginning.

To needing the application of air-conditioning or refrigeration, in some configuration, the user preferably disposes the absorption cooling device, and VAST recycle unit and/or relevant flow velocity are set, to provide required temperature and logistics to this absorption cooling device. For example be used for air-conditioning and refrigeration. Selectively, the user provides mechanical compress/expansion air-conditioning to substitute or the assisted absorption air-conditioning.

In other was used, the user provided electric energy or mechanical energy, heat energy and aircondition simultaneously by suitable configuration VAST circulation.

The power of this class associating and cooling are configured in thermoeconomics and the environment aspect is better than conventional correlation technique greatly.

In certain embodiments, the user produces excessive water (or realizing clean positive water balance) by VAST steam circulation (VAST-WS) and/or VAST economizer circulation (VAST-W). (referring to, Figure 44 for example). That is, the hydrogen in the fuel forms water in combustion process. Preferred condensation and these extra water of a recovery part are to realize clean positive water balance (net positive water balance).

For example, industrial air to 50MW (aeroderivative) example of deriving, circulate by VAST steam, under the condition of about 105% stoichiometric air stream, than β, the user can obtain clean positive water balance for all air compressor pressures of from about 10 to about 50 that calculate. Do not having under the air cooled condition, circulation also can obtain similarly clean positive water balance to VAST steam. The type of based on fuel, air compressor ratio beta, and the temperature of the ambient parameter of relative humidity and extraneous cooling fluid (for example desert air of the heat from about 7 ℃ deep-sea seawater to about 45 ℃ or higher temperature), the amount of these logistics is about 0.5 to about 1.5 times of fuel flow rate.

Dispose described VAST steam and circulate to improve the internal rate of return (IRR), simultaneously described excessive water is originated as steam, so that the sold water yield of condensation and recovery does not have about twice of the water yield in the configuration of water sale for some in the configuration.

Similarly, in this example, use about 105% stoichiometric air stream, air compressor pressure than for about 28 or higher condition under, the user can obtain the water purification balance to the circulation of VAST economizer.

Comparatively speaking, the wet circulation pattern of all prior aries all needs a large amount of supplementing water. The flow velocity of these supplementing water is about about 4 to 9 times of fuel flow rate. Compare with the supplementing water (negative water balance) that existing circulation technology CC2L, STIG, RWI, HAT are required with HAWIT, the excessive water that the VAST circulation produces (clean positive water balance) has larger environment and thermoeconomics advantage.

The configurable air cooling system of this class VAST Circulated power system. Therefore, it can be placed on Anywhere, and comes start-up system until obtain the positive water balance except the enough water of initial needs, without any need for extraneous water supply.

When VAST circulation obtains clean positive water balance (excessive water), input contain majority of particles in oxidant, fuel and the hot diluent and alloy in described condenser with described hot diluent condensation. The concentration of these components in the described excessive hot diluent of condensation is similar or be lower than the concentration of these alloys in input fuel. These alloy amounts from burner inflow decompressor are equivalent to the amount of input described fuel and the oxidant stream approximately, add the amount of the alloy that together recycles with described hot diluent (such as water).

When the alloy in these fluid-mixings was lower than described decompressor requiring under assigned temperature, the user was preferably by ejecting these alloys the accumulation of these alloys of control from formed excessive hot diluent system. For example, by discharging excessive water. In this class configuration, by replacing nearly all required water treatment facilities of conventional prior art system cost is significantly reduced.

Dispose water storage device, it is used for storing excessive recycle-water or the supplementing water that comes from the outside, and water starts before beginning or acquisition recycle-water or other supply water to help for the VAST circulation. In improved embodiment, use bubbler system (bladder system) that the P-V higher than other system is provided.

Coming to supply water with one or more feeding engines under predetermined condition fills described VAST circulation assembly or promotes house steward (header) pressure.

The temperature distribution of preferably controlling the burning fluid and/or leaving the high energy gas of burner by adding hot diluent. Preferably it is pumped in the hot system as liquid diluent. Preferably liquid and/or vaporization or overheated hot diluent is carried by one or more distributed contactors as herein described. The preferred spatial distribution that adopts the present embodiment to form water/fuel and air/fuel, this distribution is even more than routine techniques. This causes space temperature difference obviously to reduce.

In some configuration, in the flame downstream, around burner 4000, inner and along the extra nozzle of this burner configuration, to improve the conveying of water or steam.

The user preferably controls the ratio of the hot diluent that is delivered to fuel, with the temperature of control gained reactant mixture or high-energy fluid. The preferred any excessive oxidant of estimation and/or the hot diluent of gaseous state or other reactant, and each can change temperature, pressure and the thermal capacitance of the fluid of reaction temperature or high-energy fluid temperature.

For example, table 4 has shown under various water/fuel ratio makes water as the representative temperature of hot diluent gained, the #2Diesel fuel that service condition provides with about 350K (about 77 ℃ or 171 °F) for burning, compressed-air actuated amount is 110% chemical dose, its pressure ratio is about 10 (for example 10 bar), temperature is about 788K (about 515 ℃ or about 959 °F), and the relative humidity of input air is about 60%. Under the external condition (about 27 ℃ or 81 °F) of about 300K, provide input water.

Table 4 is by the temperature of water/fuel ratio control reactant mixture
					The air of the Diesel fuel (C12H26) of 350K, 110% chemical dose of 10 bar, the environment ISO condition of 788K, the water of 300K
Water/fuel (quality/quality)	Water/fuel (mol/mol)	Temperature K	Temperature ℃	Temperature °F
					0	0.176	2,230	1,957	3,555
1	1.658	2,102	1,829	3,323
					1.5	2.588	1,993	1,719	3,127
2	3.168	1,884	1,611	2,931
					2.67	4.428	1,752	1,479	2,695
3	4.975	1,692	1,419	2,586
					4	6.633	1,524	1,251	2,284
5	8.292	1,367	1,094	2,001
					6	9.95	1,236	963	1,765
7	11.61	1,119	846	1,555

For example, when about 110% excess air, preferably provide about 7: 1 water of mass ratio/Diesel#2 fuel, temperature is controlled at about 846 ℃. Similarly, preferably provide about 2: the 1 water/fuel of mass ratio that outlet temperature is controlled at about 1,611 ℃. This scope of 7: 1 to 2: 1 has covered the turbine inlet temperature scope (that is, about 900 ℃ of 1,525 ℃ of H class technology (projected H class technology) to plan of the non-refrigerated gas turbine of blade) of most commercial gas turbines

In another embodiment, preferably under the condition of about 110% excess air, provide about 1.5: 1 water/Diesel#2 fuel ratio, so that the temperature of high-energy fluid is about 1720 ℃. This is similar to the turbine inlet temperature that high temperature test-type ceramics turbo machine adopts. About 1: 1 water/Diesel#2 fuel ratio obtains about 1829 ℃ high-energy fluid temperature.

Use common thermal chemical reaction or computation fluid dynamics codes as can be known, can calculate at an easy rate ratio, different inlet conditions or recuperation of heat condition or the similar water under natural gas or other the fuel condition/fuel ratio of other temperature, other excessive oxidant or excessive gaseous diluent.

By embodiment of the present invention or in aforementioned application, carry hot diluent with the temperature of leaving the high-energy fluid of burner be controlled at be lower than about 2,073K (about 1,800 ℃ or about 3,272 °F). Described temperature is controlled at the temperature (being about 1 ℃ or about 34 °F to water for example) of the fluid diluent that is higher than cooling.

In many configurations, the mass flow of preferred hot diluent is higher than the quality of fuel flow. For example provide water/Diesel#2 be about 2: 1 to about 7: 1 water/fuel ratio with the temperature of high-energy fluid be controlled at about 1,611 ℃ to about 846 ℃ of scopes. This has covered the turbine inlet temperature scope of most commercial gas turbine decision design.

Do not causing fray-out of flame or causing the pressure in high CO discharging or the burner to swing under the excessive prerequisite that the water yield that routine techniques can be carried is limited. For example, compare less than about 1.1: 1 by water/quality of fuel. In preferred embodiments, preferred water at least about 1.5: the 1/fuel mass ratio that uses.

By hot diluent is injected combustion system 4000 and reduces excess air, the thermodynamical model of VAST circulation shows when high-energy fluid expands and cool off, even when being expanded to when being lower than atmospheric pressure, the concentration of steam can not satisfy hot diluent (steam) condensation in gas turbine. This makes the corrosion of the turbine blade that the condensate in the expansion fluid causes minimum. Comparatively speaking, make steam reclaim heat by normal expansion of condensation turbine with the recuperation of heat steam generator, can in turbine, produce diluent or the water of the condensation that makes the blade heavy corrosion, particularly under the condition of higher expansion rate and lower pressure.

In certain embodiments, preferably cool off the turbine discharging gas of expansion with the cooling agent fluid near room temperature. The extraneous cold water that passes through to provide or air heat exchanger cool off described cooling agent fluid.

The assembly of the heat of cooling

Energy conversion system has the assembly that needs cooling usually, and it usually adopts air cooling thereby causes thermal loss. In some configuration, preferably cool off this class component with diluent cooling stream and reclaim that these are rudimentary in intermediate heat. Preferably according to heat sensitivity and cooling requirement to damage assembly is sorted. Preferably the cooling according to life cycle benefit and/or damage flows to line ordering. In some configuration, preferably according to the order of heat sensitivity and economic benefit assembly is cooled off.

With reference to Figure 22, a kind of VAST circulation VAST-WS circulation as shown in Figure 3 can be configured to cools off heat generating component. Similarly, can be to being cooled off by the assembly that contains the oxidant fluid heating such as high-energy fluid or compression. According to the needs of these cooling requirements, preferably provide one or more flow dividers or one or more in the cold diluent of heat and quality transmission system 6000 supplies, warm diluent, warm diluent, diluent steam or the overheated diluent steam optionally. For example, these logistics can be obtainable cold, temperature or hot water, saturated vapor and/or superheated steam. Preferably the diluent with heat is used for inner or outside heat application.

For example, flow divider 6450 can be placed between diluent treatment system (DTS) 2010 and the low-temperature heat source. The temperature-sensitive electronic building brick that this normally generates heat and some electric assembly are such as electromagnetic transducer, transformer, frequency converter, electronic driver, electronic controller.

For example the power transfer electronic building brick is very responsive to chilling temperature, and this is higher than necessary or required value so that the temperature of described electric power connector spare rises to. By cooling stream and radiator described temperature is controlled at and is lower than 100 ℃ or similar given temperature. That the reliability that makes high temperature reduces rapidly, causes is malfunctioning, reduce validity and increase replacement cost. Yet, use the water colder than required cooling also remarkable not as reducing the effect of other assembly application cold water to the further effect of electronic device.

Preferably carry cooling secretly in the direct contact type spraying filtrations/cooling device of the coldest part of economizer, preheater, input air, direct contact type in the compressor sprayer unit, cool off direct contact type spraying centre and/or compressor between surface cool among the coldest hot diluent (for example water or refrigerant) of one or more middle use.

Preferably assess relative benefit, and between these are used, distribute described colder hot diluent according to order and the ratio of benefit.

The hot diluent (such as water) of temperature can be delivered to and need to or benefit from cooling, but temperature requirement and undemanding middle temperature-heat-source. For example, the water that is heated near 90 ℃ to 95 ℃ by heat of cooling conversion electron assembly is preferred for cooling off generator and pressure vessel subsequently.

Similarly, can dispose flow divider 6460 between low-temperature heat source and middle temperature-heat-source uses according to required hot water is sent to such as the hot water of spot heating. Similarly, another current divider 6470 is configurable is sent to burner 4000 according to required with this class hot water. Normally heating electronic package, for example generator, motor, bearing, pump and thermo-mechanical drive of temperature-heat-source in these.

Temperature-heat-source can be divided into the assembly of lower temperature in these, as makes with lubricator bearing, gear train and speed change driver (noticing that existing lubricant can be worked under 500 °F). Pressure vessel is the assembly that is heated, and it preferably is controlled at below 500 °F. Similarly, motor and generator are subject to the restriction of the solution temperature of the temperature of insulating coating and welding material.

The diluent of heat can be sent to subsequently high temperature heat source to cool off relevant assembly. For example, the heat passage in described combustion system and the expansion system. These can comprise one or more in combustion chamber bushing pipe, balance or transition zone, turbine fin (vane), turbine blade, turbine connector and one or more levels the turbine wheel cap. Flow divider 6480 is configurable between middle temperature-heat-source and high temperature heat source, is used for carrying diluent (for example steam) heat or vaporization to the high-temperature use (or utilization of steam) of correspondence.

Similarly, flow divider 6490 is configurable between high temperature heat source and burner, is used for using or the overheated diluent of steam application conveying to overheated diluent. Preferably remaining high temperature or overheated diluent are sent to described burner. At this moment, preferably it is mixed with oxidant, diluent and/or the fuel fluid of upstream, combustion zone. In some environment, preferably provide vaporization that the diluent of high flow capacity more or colder diluent make it possible to avoid described diluent or overheated. For example use the water of pressurization.

These methods have effectively reclaimed more rudimentary heat and have been recirculated to described high-energy fluid. The method of this thermal cycle has reduced uses excessive oxidant fluid heat of cooling workshop section assembly in the prior art, and by cooling off like this high-energy fluid and the problem of relaxing cycle efficieny.

The burner configuration

According to one or more required measures, in selected energy conversion system, provide and arrange burner, carry process with control burning and diluent. In certain embodiments, can use to operate and be used for carrying diluent and with diluent and the burner that contains oxidant fluid and mix, it preferably includes at least part of liquid diluent. For example, can use the burner of instructing in the United States Patent (USP) 3651641,5617719,5743080 and 6289666 of Ginter.

The fluid that is delivered to these burners is preferably controllable, with take fire and the smooth combustion operation before keep flammable mixture.

The user preferably disposes the burner that can operationally carry more diluent after taking fire. Burner with this ability can be carried the diluent that surpasses the saturated restriction of diluent common in most correlation techniques, therefore substitutes the most oxidant fluid that contains. For example, can use the burner such as the Ginter instruction in the circulation, it has overcome such as STIG, HAT (or " EvGT "), HAWIT, RWI and has united saturation of the air restriction common in the vaporize water circulation of adopting in the circulation.

More preferably select can operate to control the burner that carry in the space of diluent in described burner, thus the dilution dosage of vaporization before the control burning beginning, to keep the smooth combustion in flammable mixture and the burner. Correspondingly, described diluent is carried and preferably can be controlled the more diluent of vaporization after the burning beginning. For example, preferably use the VAST burner of instructing in the three fluid patent applications. In some configuration, these VAST burners are so that comparable conventional combustion stability limit carries more liquid diluent to the upstream of burning zone. These burners preferably dispose the horizontal space control that fluid is carried and mixed. This is so that the control of convection cell component and combustion process is stronger, thereby can more realize stable operation under the condition near the stoichiometry operation.

Preferred described burner also can operationally be carried diluent vaporization or gaseous state. For example, preferably use the burner with this ability of instructing in the three fluid patent applications. These burners preferably can be carried diluent and the liquid diluent of vaporization. For example steam and heat (or cold) water. This be so that can carry more diluent than the diluent in the circulation of prior art vaporization capacity, and gives from expansion fluid recovery and recycle the ability of more heats. Total dilution dosage that the VAST burner of for example, instructing in the three fluid patent applications can be configured to conveying is 2-4 times that dosage is diluted in vaporization. For example, such as steam and water conventional or heating. This has surpassed the quantity of steam that can be transported to burner in the STIG circulation.

Preferably with maximum can reclaim from heat recovery system 6000 and not have be delivered to burner 4000 for the vaporization diluents of other application. More preferably with keeping oxidant flammable mixture, still less and more diluent moves burner, described flammable mixture is containing fuel fluid, contain oxidant fluid and containing the diluent fluid of being pre-mixed under the fluid transport condition, be that it substitutes the incompressible diluent of more gaseous state, for example contain oxidant fluid or as the air of diluent.

Should illustrate that among the figure that the present invention provides, described burner shows with the form of thermodynamics "black box", it operationally carries mixing and inflammable containing fuel fluid, oxygen-bearing fluid and contain the diluent fluid. These schematic diagrames are not meant to order or the position that shows that diluent and fuel are carried. More specifically reagent fluid space conveying can be referring to one or more patents of three fluid patent applications, ' 191 patent application and Ginter.

More preferably use the VAST three fluid combustion devices of the transverse spatial distribution of operationally controlling fluid, instruct in the three fluid patent applications that for example replenish. Preferably this burning is configured to the cross direction profiles at least one direction control temperature. For example, the control of the radial direction of annular burner by from the connector to the turbine blade and the fin tip temperature of carrying out the high-energy fluid of described turbine distribute or section.

The preferred combustion system that operates high precision ground control fluid and fluid ratio of using as instructing in the three fluid patent applications. This makes it possible to move this burner and carries reliably peak temperature near the high-energy fluid of the design peak temperature of decompressor.

Preferably control the cross direction profiles that fluid is carried, and the transverse temperature distribution is controlled at the approaching temperature distribution that designs. This is so that can move under higher mean temperature in the range of uncertainty that maintains simultaneously the space temperature design.

Such as what instruct in the three fluid patent applications that replenish, preferably dispose and control described burner, so that burning near chemical dose by the lateral fluid component in numerous zones of described burner outlet. This component of preferred control to be substituting the fluid diluent that contains oxidant, and at least a alloy is controlled at is lower than required limit. For example, carbon monoxide, fuel element remaining or partial reaction, and nitrogen oxide. This is so that can move under near stoichiometric condition when satisfying the disposal of pollutants limit.

Concrete circulation

VAST water circulation: VAST-W

The embodiment of described thermodynamics circulation can be configured (VAST-W) shown in figure 02.

In this configuration, part can be comprised in the liquid diluent F275 direct injection burner 4000 of H2O. As shown in the figure, can use the diluent heat exchange subsystem 6020 (also referring to Figure 27) with economizer 6500, always reclaim heat among the expansion fluid F420 of self-expanding machine 5100 with diluent flow F429. In certain embodiments, described diluent can be directly through flow divider 6310 and 6320 and pump 2200 and 7800 from diluent processor 2300.

Can as required or require to add or remove pump, flow divider and mixing valve to obtain results needed. Although be shown as by variable proportion or flow divider and control flow, be to be understood that the combination of other assembly or assembly also can obtain similar result. For example, by using one or more controlled valves, pump and flow rate limiting device.

Along with liquid diluent is added in the combustion chamber 4100, generated diluent steam, and it mixes formation high-energy fluid F405 with combustion product. In certain embodiments, can reclaim with the economizer 6500 in the diluent heat exchange subsystem 6020 in after the decompressor 5100 or downstream heat in this process.

Reclaim diluent among the described expansion fluid F420 by will be directly being sent to diluent recovery system 6010 from least a portion of the expansion fluid F420 of decompressor 5300. Other embodiment makes this expansion fluid by economizer 6500 before can being delivered to diluent recovery system 6010 at the diluent F460 with cooling.

In diluent recovery system 6010, expansion fluid is processed to reclaim described diluent, and in certain embodiments, this diluent is recycled back described thermodynamics circulation. In certain embodiments, described diluent recovery system disposes surface condenser 7400 (as shown in figure 34). Can use cooling device 7600 from being used for the heat that in the cooling fluid of surface condenser 7400 cooling expansion fluids, sheds. Can remove the diluent that reclaims from surface condenser 7400, and if it need to be recycled back the F295 of system. In certain embodiments, this can pass through diluent treatment system 2010.

In another embodiment, the diluent recovery system 6010 of Figure 35 can separate described diluent with direct contact type condenser 7500 from described expansion fluid. In this configuration, described cooling fluid directly contacts with described expansion fluid, and in the process of removing described diluent. Subsequently described diluent and cooling fluid are recovered into F240, and in certain embodiments, before being reused for direct contact type condenser 7400, cool off with cooling device 7600.

In the embodiment of diluent recovery system, the cooling fluid after the described heating and the diluent of recovery can be used for needs or require the application of heat. This cooling and diluent fluid can be distributed to these application, and if necessary, can return in certain embodiments to loop back in the described system. As shown in figure 36, in one embodiment, will cool off with the diluent flow body for district heating.

In certain embodiments, can be with described diluent and the cooling fluid circulating involuting system F295 that reclaims from described direct contact type condenser. In certain embodiments, this need pass through diluent treatment system 2010.

In some embodiment of this thermodynamics circulation, but the recompression machine 5300 in the application drawing 02. By this recompression machine, described expansion system can have higher expansion ratio, and can reclaim more merit W580 from high-energy fluid F405. Then diluent (expansion fluid) F460 of expansion fluid and at least part of removal can be delivered to recompression machine 5300 from the diluent recovery system. Subsequently, recompression machine 5300 makes the pressure of this fluid near environmental pressure, thereby so that it can be discharged from system.

VAST water and steam circulation: VAST-WS

Shown in figure 03 (VAST-WS), the embodiment of VAST dynamics circulation can be configured to liquid diluent and the diluent steam that uses one or more heat exchangers heat to be recycled to heating from the high-energy fluid that expands.

In this configuration, preferably operative liquid diluent and part steam diluent are delivered to burner 4000. (it can comprise the fluid water of hot water and steam-like). As shown in figure 29, can use diluent heat exchange subsystem 6020, being used for the expansion fluid F420 of self-expanding machine 5100 heats diluent, and wherein said heat exchanger is shown as economizer 6500, evaporimeter 6600, superheater 6700. Described diluent is shown as by diluent treatment system 2300 and provides, and is delivered to diluent recovery system 6010 and be shown as from the expansion fluid of decompressor after recuperation of heat.

Along with diluent is added in the combustion chamber 4100, generated diluent steam, and it mixes formation high-energy fluid F405 with combustion product. In case this high-energy fluid expands in decompressor 5100, the thermal expansion fluid F420 that produces can be delivered to heat exchanger array or diluent heat exchange subsystem 6020, enter the diluent of combustion system 4000 with heating.

Among Figure 29, preferably make the hottest expansion fluid by heat exchanger 6700, its reception is near the diluent steam F251 of the heat of boiling point, and makes it overheated before it is delivered to combustion system 4100. In certain embodiments, heat exchanger 6600 can receive the liquid diluent of heat, and make its boiling with the expansion fluid of heat, by the expansion fluid from the upstream before the superheater heat exchanger 6700, or produce steam from the expansion fluid of decompressor 5100 in certain embodiments.

Can before being heated to higher temperature with liquid diluent, boiling heat exchanger 6600 use economizer.

Such as Figure 28 and shown in Figure 29, the VAST circulation can be configured to before the heat exchanger array and operationally extracts afterwards hot diluent and use to be used for other heat or cooling. In certain embodiments, can between heat exchanger, extract as shown the diluent of heat.

Can use in certain embodiments the diluent of this heat, be introduced into other zone of combustion system 4000 or the circulation of described thermodynamics when at least part of described diluent.

Expansion fluid from economizer 6500 can be delivered to diluent recovery system (DRS) 6010. In diluent recovery system 6010, this expansion fluid is processed the described diluent of recovery, and in certain embodiments, this diluent is looped back described thermodynamics circulation. In certain embodiments, the diluent recovery system may be configured with surface condenser 7400 as described in Figure 34. Can use cooling device 7600 from being used for the heat that in the cooling fluid of the described expansion fluid of surface condenser 7400 coolings, sheds. Can remove the diluent that reclaims from surface condenser 7400, and if it need to be recycled back the F295 of system. In certain embodiments, this can pass through diluent treatment system 2010.

In another embodiment, the diluent recovery system 6010 of Figure 35 can separate described diluent with direct contact type condenser 7500 from described expansion fluid. In this configuration, described cooling fluid directly contacts with described expansion fluid, and in the process of removing described diluent. Subsequently described diluent and cooling fluid are recovered into F240, and in certain embodiments, before being reused for direct contact type condenser 7400, cool off with cooling device 7600.

In the embodiment of described diluent recovery system, the cooling fluid after the described heating and the diluent of recovery can be used for needs or require the application of heat. This cooling and diluent fluid can be distributed to these application, and if necessary, can return in certain embodiments to recycle back in the system. As shown in figure 36, in one embodiment, will cool off with the diluent flow body for district heating.

In certain embodiments, described diluent and the cooling fluid that reclaims from described direct contact type condenser can be recycled back the F295 of system. In certain embodiments, this need pass through diluent treatment system 2010.

In some embodiment of this thermodynamics circulation, but the recompression machine 5300 in the application drawing 02. By this recompression machine, expansion system can have higher expansion ratio, and can reclaim more merit W580 from high-energy fluid F405. Then diluent (circulation of the expansion) F460 of expansion fluid and at least part of removal can be delivered to recompression machine 5300 from described diluent recovery system. Subsequently, recompression machine 5300 is promoted to the pressure of this fluid near environmental pressure, thereby so that can be with its discharge system.

Some advantage of this VAST steam circulation (VAST-WS) for example is presented among Figure 38, is operated in the industrial turbines that the air of 1300 ℃ 50MW is derived. Suppose that fuel and electricity rates are the average industrial gas of the U.S. and the electricity rates that USDOE (US Department of Energy) announced in 2000. Identical equipment assembly cost equation is used in all circulations, its for Traverso and Massardo 2003 (submission is published in International Gas Turbine Institute Turbo 2004) that develop. (these are similar to Traverso, and 2002 comparative analysis has some adjustment. )

It should be noted that with the circulation of conventional prior art and compare that described VAST steam circulation has suitable efficient, but basic capital cost reduces significantly. In this example, under the pressure ratio of these conditions and about 20-30, in foundation load and 8,000 the man-hour/internal rate of return (IRR) (IRR) of described VAST steam circulation during year is about 24%, and fractional load (50%) and 4,000 the man-hour/IRR is about 12% (a spraying intercooler is arranged) between low pressure and high pressure compressor during year.

Under these conditions, to foundation load and 50% load, STIG circulation compared to existing technology, the internal rate of return (IRR) (IRR%) of this VAST steam circulation example has improved 2-4 percentage (being the high approximately 20%-40% of IRR%). Similarly, by contrast, carry out two press water laterals of prior art at the 50 MW turbines in similar year 4000-8000 hour man-hour and close the internal rate of return (IRR) that circulation (CC2L) can only obtain 2%-4%, and VAST steam to circulate be 12%-24%.

RWI, HAWIT are compared in described VAST steam circulation and the HAT circulation has similar advantage. (referring to, Figure 38 for example).

VAST steam circulation (without the air cooling) with the cooling of steam blade

Use the circulation of described VAST steam, flow and/or the temperature of hot diluent steam or overheated hot diluent steam preferably is set. Preferably with one cooling agent as decompressor thermal technology section in these logistics. For example, one or more turbine fins, blade and guard shield. Compare as decompressor thermal technology section cooling agent with using compressed air, this has significantly improved the efficient of system. This has also reduced system cost, and has improved the thermoeconomics (referring to, Figure 49 for example) of system.

For example, the gas turbine of the 50MW industrial air of operation VAST steam circulation-derive, the steam cooling substitutes the air cooling, can make the thermal efficiency bring up to about 53.3% by about 51.3%. This hypothesis is returned this steam that is heated the burner of described decompressor upstream after thermal technology's section of cooling decompressor (for example turbine blade and fin).

In improved configuration, come heat of cooling workshop section assembly (for example blade) with steam, and subsequently it is delivered in the high-energy fluid stream in the turbine. In these relevant calculating, this combination meeting is brought up to 51.3%-53.3% with efficient.

In the VAST circulation, suppose that the excess air consumption for the turbine blade cooling is about under 110% stoichiometric condition for 18% of the air mass flow of burning. Therefore, eliminate described excessive compressed air and the compressor size in the VAST circulation can be reduced about 15%.

In these relevant calculating, under the condition of the about 20-30 of air compressing pressure ratio, in this VAST circulation, substitute air with the steam cooling and cool off, reduced equipment cost, and it is about 2% that the internal rate of return (IRR) is improved, and is increased to about 14%IRR from about 12%IRR.

VAST water and steam circulation: VAST-WSR with the backheat circulation

(VAST-WSR) disposes the embodiment of thermodynamics circulation as shown in Figure 4. This is to adopt the VAST-WS circulation to come with the embodiment that contains oxidant fluid recovery heat.

Shown in figure 32, diluent heat exchange subsystem 6020 comprises gas-gas-heat exchanger or regenerative apparatus 6800 and packed layer humidifier 7300 in this configuration. Further embodiment can comprise the second economizer 6510 and aftercooler 6900.

Figure 37-46 has shown advantage and the result of these circulation embodiments.

The oxidant supply system

Oxidizer source

In many embodiments, use to contain oxidant fluid, normally oxygen-bearing fluid or oxygen, as a supplement altogether-reactant (co-reactant) fluid. Some contains oxidant fluid and comprises one or more hot diluents, such as nitrogen, water, carbon dioxide with such as inert gas of argon etc.

Many embodiments adopt air to provide oxygen as the described oxidant fluid that contains to combustion system 4000 or burner. In certain embodiments, preferably the variation of air humidity, temperature and pressure is compensated.

In embodiments, use liquid oxygen, the oxygen by evaporating the liquid oxygen preparation, the oxygen that electrolysis forms, the oxygen that solid electrolyte separates or the oxygen for preparing by other method.

Conventional oxygen fuel combustion produces awfully hot high-energy fluid F405. This high temperature is so that be difficult to keep long-lived burner bushing pipe. In certain embodiments, lean on very closely when hot diluent distributor pipe array distribution fuel and hot diluent. This has limited the temperature of high-energy fluid F405 greatly. In some configuration, use liquid oxygen, preferably carry this liquid oxygen, the uniformity coefficient that mixes to improve fuel, oxidant and diluent by directly contacting pipe.

This class embodiment has obtained lower peak value fluid temperature (F.T.), so that easier manufacturing can be stablized the combustion system 4000 of tolerance combustion process. Similarly, described hot diluent distributor pipe and radiation shield fin (fin) greatly reduce the heat flux that described fuel distributor pipe bears.

In certain embodiments, preferably make the liquid oxygen evaporation by heat exchanger with the inner burning fluids that produce or expansions that come from the outside or two kinds of sources of VAST circulation, hot diluent, at least a heat or the electric energy in the district heating fluid.

Some embodiment is used " richness " oxygen air, and its oxygen concentration is brought up to the level that is higher than normal air by one or more enrichment methods. These methods comprise the concentrated system of transformation zeolite and the concentrated system of vacuum transformation. Also can use film oxygen coalescence method. Owing to use the oxygen burning, (perforated) fuel of porous and contain oxidant fluid distributor pipe array and greatly limited ignition temperature and simplified the burning design.

Filter

With reference to Figure 12, preferably in oxidant fluid processor (TRE) 1200, use the atomizing hot diluent of contactor filter liquid towards that directly circulates to spray, to remove particulate and the fiber in the oxidant fluid of containing of input, for example air of input. This direct contact type filter preferably adopts the direct contactor of the porous of instructing in the patent application of ' 191. These preferably the are configured to multichannel spraying system shown in ' 191 patent application Figure 82. The diluent that uses does not need to have the high-quality identical with the diluent that enters burner. It can be from by removing by filter less than the particulate of distribution hole size the diluent that directly reclaims. Significantly improved the alloy load that enters burner if spraying is carried secretly, then described diluent need carry out section processes. The liquid diluent (such as cold water) of collecting can return diluent treatment system 2010, maybe can extract out for other application or discharging by diluent tapping equipment (DWD) 8500 to be used for energy conversion system. The preferred alternative or assist gas/air cleaner of this spraying filtration that uses.

In some configuration, preferably provide the differential pressure sensor to monitor pressure drop by described input gas/air cleaner, to determine when cleaning or to replace this air cleaner. In certain embodiments, use a plurality of filters with volume control device (valve, air throttle etc.), for example can be at the wiretap input source when a filter is waited for maintenance, this filter to be keeped in repair since particulate and other buildup of material so that differential pressure increases, improved flow resistance thereby reduced total cycle efficieny.

Preferably cool off and filtered air with cold liquid diluent. This filtration has reduced the fiber accumulation rate in compressor 1300 (for example on compressor fin and the compressing tablet) and decompressor 5100 (for example on decompressor fin and blade). Air cooled off give compressor higher capacity, particularly on date of sweltering heat. Filtration has reduced the speed of compressor and decompressor fouling, thereby has reduced the maintenance downtime, the cleaning cost, and balance compressor and efficient. It has reduced the pressure drop of passing through fluid (gas/air) filter, has reduced the pump power of compressor.

When using water spray device with the direct contact type filter to come filtered air, diluent before the preferred control burning is carried, compensate the variation of moist composition, this changes from the humidity variation and from using diluent by atomizing direct contact type filter.

Compressor

In the medium-to-large Gas Turbine Power System, compressor is the equipment of independent investment maximum in the high compression ratio system, and cost surpasses decompressor. In than the low compression ratio system, compressor remains very large investment. With reference to Fig. 5, the configurable compressor (CP) 1300 with a series of a plurality of compression sections of user comes to contain oxidant fluid from oxidizer source 1100 receptions, thereby realizes the overall compression ratio that it is required when this fluid is delivered to combustion system 4000. With reference to Fig. 7, the user preferably provides and contains the diluent fluid and reduce the used excessive amount that contains oxidant fluid by the means described in the patent of one or more the present invention, three fluid reactor patent applications, ' 191 patent application and aforementioned Ginter. For example, use can be near the burner of working under the stoichiometric condition, such as Ginter VAST burner or VAST three fluid combustion devices. Auxiliary these measures, the user preferably changes the compressor size, reduces the fluid capacity of described compressor with respect to turbine. So significantly reduced the cost of compressor and energy conversion system.

For example, be reduced to about 110% stoichiometry by preferably compressed air being flowed from the 334% stoichiometry flow (about 1300 ℃) of ultra-poor burning, the flow by described compressor partly can be reduced about 67%. Similarly, preferably by providing the diluent such as steam and water to substitute the compressed air that is generally used for cooling off decompressor thermal technology section (such as turbine blade, fin and guard shield (shroud)). By these measures, substituted about 10%-18% be generally used for cooling off decompressor contain oxidant fluid (for example compressed air). These measures can make the size of described compressor reduce about 67% to about 72%. The reduction of compressor size significantly reduces the capital investment that is converted to the VAST circulation time.

In certain embodiments, the user preferably uses the method that the compressor size reduction is saved cost under wirking pressure, improving total effective compression ratio β, and then improves the turbine expansion ratio, thereby improves system effectiveness. In improved embodiment, compare common configuration, supply many decompressors with identical a plurality of compressors.

The user preferably provides basic low pressure compressor (base low pressure compressor) (LPC) 1310 to pressurize to containing oxidant fluid.

In some configuration, the user preferably adds the pressure that contains oxidant fluid that one or more high pressure compressors (HPC) 1350 are brought up to the compression of burner 4000 and decompressor 5100. The overall pressure ratio β that this pressure ratio that makes the pressure ratio β of low pressure compressor multiply by each high pressure compressor obtains improves.

In certain embodiments, the user preferably regulates the pressure ratio (for example comprising low pressure compressor 1310 and high pressure compressor 1350 and recompression machine 5300) of one or more compressors, controls the overall expansion ratio of high-energy fluid. By it being controlled adjust clean specific power, system's power efficiency, system's overall thermal efficiency and/or reducing one or more in the Thermoeconomic Cost of life cycle.

For example, consider that configuration is used for the gas turbine of the 50MW of VAST-WS (circulation of VAST steam), between low pressure and high pressure compressor, use water spray formula intercooler, 1300 ℃ turbine inlet temperature work, use average industrial natural gas cost and the electricity rates of USA 2000. The derive mean value of efficient of turbine of the air that turbine efficiency is got the 1990 class technology of GE and Rolls Royce.

The pressure ratio of the typical low pressure compressor of some of this configuration, high pressure compressor and recompression machine distributes such as Figure 47 and shown in Figure 50, and the air compressor pressure ratio is 10-44.

In a similar manner, in routine is sprayed the turbine configuration that intercooled industrial 50MW air derives, to about 30 contain oxidant fluid pressure ratio β, the low pressure compressor ratio of configuration is about 3.16.

Similarly, to being about 10 air compressor pressure than β, preferably the ratio with low pressure compressor is made as about 2.53. Air compressor pressure to about 44 preferably is increased to about 3.64 with this ratio than β.

Similarly, in the turbine configuration that the industrial 50MW air of routine is derived, the pressure ratio β that contains oxidant fluid is about at 30 o'clock, in certain embodiments, the user preferably is about 9.47 (referring to, Figure 47 for example) with the ratio setting of high pressure compressor.

Similarly, to being about 10 air compressor pressure than β, the ratio that preferably will recompress machine is made as about 3.94. (referring in the expansion system to the recompression machine discussion). Air compressor pressure to about 44 preferably is reduced to about 2.2 with pressure ratio β than β.

Should be noted that the preferred result by these atomizing intercoolers, the pressure ratio of described two kinds of compressors is respectively 3.16 and 9.47, the square root or about 5.47 that its optimum pressure ratio that obviously is different from the effects on surface intercooler is overall pressure ratio.

The user preferably regulates the ratio of recompression machine 5300 to improve or to optimize the economics (for example higher internal rate of return (IRR) %) of system, and it approaches the optimum thermal efficiency. (referring in the expansion system to the recompression machine discussion). The internal rate of return (IRR) is shown as the parabola of the reversing of inclination to the curve (Figure 38) of the thermal efficiency, when recompression when being higher or lower than the configuration that approaches by the definite high internal rate of return (IRR) (IRR%) of used hypothesis, economic benefit and the thermal efficiency reduce simultaneously.

For example, in the turbine configuration that the industrial 50MW air of routine is derived, the pressure ratio β that contains oxidant fluid is about at 30 o'clock, in certain embodiments, the ratio setting that the user preferably will recompress machine is about 2.6. That is, the pressure of (condensation) expansion fluid of the cooling of recompression machine entrance is about 38% (referring to, Figure 47 for example) of ambient pressure.

Similarly, to being about 10 air compressor pressure than β, the ratio that preferably will recompress machine is made as about 3.9. Air compressor pressure to about 44 preferably is reduced to about 2.3 with this pressure ratio than β. That is, the pressure of the expansion fluid of the condensation of recompression machine entrance is about 25.6% (1/3.9) to about 44% (1/2.3) of ambient pressure. (for example atmospheric %, or about 26-44kPa).

In certain embodiments, by preferably substituting gas compression with liquid compression, make with high-energy fluid be delivered to described entrance to the required total pumping merit of decompressor entrance significantly reduce (referring to, for example Figure 42 and Figure 48). So significantly having improved can be from the net power (IRR as shown in figure 43) of system's acquisition. That is, total turbine output deducts all pumping merit and loss in efficiency. Accordingly, reduced flow by gas compressor.

Reduce simultaneously the measure that contains oxidizer flow rate by improving system's net power, improved the system net power to the ratio of the mass flow by compressor outlet, or the clean specific power of compressor outlet (total turbine output deducts the pumping power of compressor and pump again divided by the mass flow of the fluid that passes through compressor outlet, and it comprises the water from relative humidity, mist, water entrainment, inner compressor water spray device or middle compressor water spray device). This has reduced the compressor capital investment corresponding to per unit net power of carrying. With reference to Figure 39, clean specific power mapping can show the benefit that the clean specific power of these compressor outlets promotes intuitively to compressor outlet by system's thermodynamic efficiency (%LHV basis). Figure 39 shown LHV circulation thermodynamic efficiency % to the clean specific power of compressor outlet (kW/ (kg/s) or curve kJ/kg) (and the mass flow that the net power that namely represents with kW or kJ/s represents divided by kg/s be equivalent to the compression unit mass contain oxidant fluid or air than merit kJ/kg). This contrast has VAST-W and the VAST-WS circulation of surface condenser, and the VAST-WS circulation with direct contact type condenser. " wetting " that these VAST circulate under a plurality of pressure ratio β of 10-40 further with main prior art loops comparison, for example at 50MW, and TIT=1300 ℃. Should illustrate, the circulation of each described prior art is extended to the saturation of the air limit of the compressor that uses corresponding adjusted size, comparing conservative comparison, and not be only the compressor surge limit to routine.

Should illustrate that in using the prior art of ultra-poor burning, the flow by compressor is similar to the mass flow by turbine usually. Yet in the described VAST circulation of prior art " wetting " circulation neutralization, the flow that leaves the compressed air of compressor and water vapour is significantly less than the mass flow by decompressor or turbine. In " wetting " circulation, the clean specific power of turbine is burnt system apparently higher than conventional fuel-sean. In Figure 39 and Figure 40, shown respectively the clean specific power of this compressor outlet and the clean specific power of turbine inlet, thereby advantage and the prior art of clearly these parameters being given the VAST circulation compare.

VAST-W (VAST water circulation) is delivered to described burner with hot water. When pressure ratio β rises to approximately 50 by about 10, the clean specific power of compressor outlet of VAST circulation 2 obviously rises to about 1200kJ/kg (kW/kg/s) from about 1020kg/kg (kW/kg/s). This is corresponding to be promoted to about 51.3% with the LHV cycle efficieny from about 43.7%.

Similarly, VAST-WS (circulation of VAST steam) is conveyed into described burner with steam and water simultaneously. It is that to be promoted to pressure ratio β be about 1200kJ/kg (kW/kg/s) of 40 o'clock for about 1120kg/kg (kW/kg/s) of 10 o'clock with the clean specific power of compressor outlet from pressure ratio β similarly.

With further reference to Figure 39, by comparing, " wetting " circulation (STIG, HAT, HAWIT, RWI and CC2LP) of the prior art of all evaluations demonstrates the clean specific power value of the compressor outlet that is lower than about 840kJ/kg (kW/kg/s). When the about 30-40 of pressure ratio β and similar LHV cycle efficieny, compare HAWIT and HAT circulation, these two kinds of VAST circulations of VAST-W and VAST-WS make the clean specific power of compressor outlet promote about 50%. The advantage that this has proved the VAST circulation can surpass the limit of the air saturation of diluent interpolation, and oxidant fluid (the being air) amount that contains that correspondingly will compress is reduced to about 110% or lower from surpassing about 150% of stoichiometric air flow.

In an initial calculation that circulates with the VAST of economizer, suppose water is forced into 165 bar. In VAST steam generation circulation, reduced this water injection pressure. By reducing excessive water discharge pressure, can improve system effectiveness, IRR% and electric cost.

An embodiment of VAST steam circulation (VAST-WS) can be configured to does not use compressed air cooling turbine machine blade, and corresponding change compressor size. When working under the stoichiometric condition, this has improved the clean specific power of compressor outlet. For example be about 10 at pressure ratio β, AIR Proportional λ is 1.05 o'clock relatively, and the clean specific power of compressor outlet is promoted to about 1380kJ/kg (kW/kg/s). When pressure ratio β was increased to about 50, the clean specific power of this compressor outlet was brought up to about 1480kJ/kg (kW/kg/s). Use in the VAST-WS circulation of the compressor of 1990 technology and turbine in supposition, these measures with system effectiveness from about pressure ratio β be 10 o'clock about 49.6% bring up to pressure ratio β be about 50 o'clock about 53%.

Lower entrance and exit loss

Turbulence in the time of will containing in the circulation of oxidant fluid suction thermodynamics has caused pressure drop and has reduced system effectiveness. In outlet similar turbulence mixing and the pressure loss are arranged. For example, prior art usually hypothesis in have an appointment 1% pressure drop of air intake, discharging or chimney (stack) have in addition 1% pressure drop (referring to, The Gas Turbine Handbook for example, 2003, LeFebvre 1998, or Dixon 1998 etc). Because compressing mechanism is into about 65% net power, therefore in ultra-poor combustion system, this entrance and the loss of discharging diffuser account for general power about 1.3% or net power 3.7%.

In certain embodiments, preferably use described preferred diluent to substitute most of excessive gaseous state as the hot diluent in the combustion system and contain oxidant fluid. For example, the user has reduced air mass flow about 67%, make λ from about 334% of stoichiometric ratio be reduced to stoichiometric ratio about 110% or lower.

Therefore, in preferred embodiments, the user has reduced about 67-72% or more with main entrance and the parasitic diffuser of outlet pressure-volume (parasitic diffuser) loss. For example, be reduced to approximately 0.67% from 2% of general power, or be reduced to 1.9% of about net power, suppose that less compressor needs about 35% general power. Thereby, preferred VAST embodiment make entrance and discharging diffuser cost about 67-72%, and make the diffuser power loss be reduced to about 1.9-1.6% from about 3.7% of net power. That is, single this net power that can save about 1.8-2.1%.

By lower entrance and exit flow, the user can reduce the line size of entrance and diffuser size with adapt to less enter the VAST circulation contain the oxidant fluid flow. This has reduced capital investment and space and floor space demand.

In improved embodiment, the user preferably increases length and the shape of entrance and outlet diffuser, with the design raising diffuser efficient of relative prior art. Conventional fuel-sean is burnt system relatively, and this has reduced the parasitic pumping loss of pressure-volume.

In improved embodiment, the user can add and control at least one air throttle or valve is controlled the inlet flow rate that enters described compressor. This for example reduces the decompressor running power so that can reduce air mass flow and the compression power of carrying.

With reference to Fig. 6, in improved embodiment, the user can add pipeline and come in the bypass compressor 1300 some to contain oxidant fluid, around combustion system 4000 to decompressor cooling system 5020, to cool off one or more decompressors. Similarly, with reference to Fig. 7, the user can extract the output of compressor formation similarly, and part is delivered to decompressor cooling system (ECS) 5020. In the 50MW embodiment of estimating, flow to flow that decompressor is used for cooling and be assumed to 10.7% of mass flow by decompressor. Described bypass pipe can comprise that air throttle/valve controls the excessive oxidant fluid flow as cooling agent.

Compressor/combustion system bypass flow can be used as for subsequent use or auxiliary of the burning fluid that use to expand, for example is used for economizer.

Owing to there is entrance and exit loss, in improved configuration, by preferred reduction entrance contain the oxidant fluid flow, the user has reduced the parasitic pumping loss by the inlet gas filter similarly. For example make conventional air intake filter loss reduce about 67-72% or more.

By the inlet flow rate that greatly reduces, the user preferably adjusts the size of inlet filter area according to inlet flow rate. Because filter capital investment is lower, size and cost of floor space are lower, and therefore parasitic pumping cost, filter replacement and labor cost reduction have saved net present value (NPV) greatly so that the life cycle operating cost significantly reduces.

When obviously saving, in improved configuration, preferably improved the filter cross-sectional area of unit gas flow, and made parasitic entrance filter pressure loss and parasitic pressure-volume be reduced to optimal value near VAST circulation life cycle.

Filter

By preferably reduced the oxidant fluid that contains of entrance with respect to conventional system, in certain embodiments, the user has significantly reduced the amount of the particulate (fiber, dust etc.) that is entrained in the energy conversion system. For example with respect to the ultra-poor burning of routine (be O2 15%), reduced about 67-72% or more in escaper.

In some configuration, the user preferably makes the air of entrance be lower than 150% or the how stoichiometric air mass flow that usually adopts in the system of prior art, these prior aries adopt the air of the wetting described compression of water, for example STIG, HAT, HAWIT, RWI, EvGT and other wet circulation, the amount of the diluent of wherein carrying are subject to containing the restriction of the saturation degree of oxidant fluid. For example, in some configuration, the λ from about 150% is reduced to about 110% λ or lower, and the water yield of wherein carrying is subject to the air saturation restriction. Compare with the wet circulation of those prior aries, but this makes the air of entrance reduce about 27% with relevant filter particulates load capacity.

With reference to Figure 12, the user preferably is provided for the filter plant that contains oxidant fluid (air of entrance) of entrance. Operating near stoichiometric air mass flow, and preferably reduce or eliminate the compressed air cooling by preferably, compare with conventional system, the user can make the cost of air filter unit about 65% to 72%. The user preferably utilizes the part of these saving, and improve the filtration of intake air by increasing certain capital cost, to reduce the consumption of life cycle, for reducing pressure drop, reduce the compressor dirt, raise the efficiency, and corresponding reduction operation and maintenance expense.

In certain embodiments, as instructing in the patent application of ' 191, the user preferably provides the direct contact type induction system that diluent is sprayed into containing in the oxidant fluid of entrance. For example, the air that is used for cooling and/or filtration entrance. Compared with prior art, these measure optimization ground have reduced filter pressure drop and pumping merit. They also provide direct contact type cooling air stream (Cooling Air flow). The size of the improved filter of preferred this class of configuration, and operation reduces the compressor fouling, reduces the compressor cleaning, improves compressor efficiency and reduce the Life Cycles expense.

The turbine fouling reduces

By making the oxidant inlet flow reduce about 67-72% or more, relatively ultra-poor burning, the user has reduced the degree of the turbine fouling that is caused by the particulate of carrying secretly in the oxidant fluid of inputting. This has reduced the cleaning of turbine blade.

The cooling of compressor and compression process

With reference to Fig. 8, the user preferably uses one or more measures and cools off the just compressed diluent fluid that contains. In Figure 84 of ' 191 patent application, instructed before the compressor formation and/or among a plurality of positions carry out similar cooling provision. This cooling provides the compression process of " similar isothermal ", and has reduced work done during compression. Described cooling preferably before the compression section, inner or between carry out. In some configuration, can use aftercooler.

Such as Fig. 8 and shown in Figure 9, the user preferably provides the surface heat exchange containing oxidant fluid and contain between the fluid of colder diluent fluid or other diluent. In some configuration, shown in the lower part of Fig. 8, the user preferably uses one or more surperficial intercoolers. These help to improve system effectiveness and increment current density. Based on less oxidizer flow rate, the size of these surface heat exchanger systems estimate to can be fuel-sean burn system the intercooler size 1/3. Adopt single surface heater between than low pressure and higher pressure compressor, expectation can make cycle efficieny improve about 1-2 percentage point. Efficient difference between this similar and HAWIT and the HAT circulation (referring to Traverso, 2001; With Traverso ﹠ Massardo 2002). By intercooler configuration of this class surface is provided, estimate that intercooled VAST steam circulation configuration can have near the HAT circulation and unites the efficient (referring to table 5) of circulation.

Table 5 heat-exchanger surface amasss (1300 ℃)
									STIG	HAT	HAWIT	RWI	VAST-W	VAST-W	VAST-WS
β
		30	30	30	30	60	30	25
									HX M 2	HX M 2	HX M 2	HX M 2	HX M 2	HX M 2	HX M 2
	REC		3092.11	3163.41	3,081.31
SH									444.13
	EVA	1527.13
ECO									1192.27	10299.00	5482.71	672.24	5469	5827.45	3882.26
					301.88
FGC-Maffo											2840.28
	FGC-other					3400	2115.87	3687.10
The gross area									3164	13391	11486	4055	8869	7943	7569
	Clean output (50MWe)	50	50	50	50	50	50	50
Area/output (M2/MWe)									63	268	230	81	177	159	151

With reference to Figure 13, in some configuration, the user preferably contains liquid state one or more positions that the diluent fluid directly injects the compressor formation. This injection is cooled off by the latent heat of evaporation and absorption. The diluent of described vaporization has increased the volume of described logistics. Compare with surface heat exchanger, this method only needs more cheap system, but so not high to the raising effect of efficient.

In Fig. 2, Fig. 3 and Fig. 4, shown single atomizing intercooler, schematically represent the diluent cooling device of embodiment. Shown in the table 4 that the pressure ratio λ that regulates between the first and second compressors improves the effect of efficient or system cost. This shows pressure and cooling agent dilution method according to the particular implementation scheme that is used for configuration VAST circulation, the size of required low pressure compressor can from β be 60 VAST-W compressor the combination cost 1% change to β be 25 VAST-WS circulate 38%. When only providing a kind of diluent to inject cooling stream, in high-pressure system, preferably it is disposed the first compressor section (or between first and second), so that all follow-up workshop sections benefit from the fluid of cooling. The configuration of use low pressure can be configured as along about 1/3 of described system path. Similarly, preferably use the direct contactor shown in Figure 16 such as ' 191 patent application that diluent is entrained into the suction port of compressor.

More preferably, as shown in Figure 8, the user is that each compression section C1, C2...CN are equipped with the spraying intercooler. The user preferably controls the injection parameter of described fluid, and to carry the vaporizable diluent to each section, its input quantity approximates can be in the amount of next section evaporation. The preferred fluid pressure drop of adjusting the bore dia in the direct contactor and passing through described hole is to produce the droplet of rapid evaporation. Preferably will evaporate apart from the distance of electing as between the section of approximating and the section. Preferred drop is of a size of can be with the logistics campaign around described fin and blade. Similarly, be configured as enough little size, not significant collision erosion during with and the collision of compressor assembly certain when drop.

These estimate the preferred collocation method of instructing in three fluid patent applications and ' 191 patent application that adopts, with the difference of the cross direction profiles that adapts to described compressor inner oxidizing agent fluid velocity. The diluent of useful heat improves boil-off rate, and cooling still is provided simultaneously. In last workshop section, the Fluid Volume of conveying can surpass can be by the amount of compressor outlet evaporation. Remaining drop can be less than the drop that usually forms in sprayer. When configuration and control burner, these are preferred.

Whether the preferred liquid of noticing that observation is injected is containing the fully evaporation of oxidant fluid stream. When shutdown system, preferably make compressor not have to move a period of time in the reinforced situation of spraying, so that its possibility dry and the reduction corrosion. As shown in figure 13, when excessive liquid diluent sedimentation and when in compressor, accumulating, can in the compressor formation, dispose " overflow (overflow) " tapping equipment.

As shown in figure 10, the user preferably uses surface heat exchanger 1900, and by dispelling the heat to environment F670 such as water or air cooled mode. More preferably, as shown in Figure 8, will be recovered in the coolant flow from the heat of cooling process and recirculation. With reference to Figure 11, the user can use direct-contact heat exchanger 1700 to cool off by the oxidant fluid F102 that contains that directly vaporizable is contained diluent fluid F270 injection compression, contains oxidant fluid F103 to form moistening compression. The direct contactor of instructing in ' 191 patent application that this direct heat exchanger preferably uses. For example shown in Figure 30, some user uses the combination of one or more above-mentioned cooling devices.

VAST steam circulation (VAST-WS) with the cooling of decompressor steam

In some configuration, the user preferably uses the hot assembly of steam cooling decompressor and substitutes at least part of preferred whole excess air that is generally used for cooled blade. Be usually used in cooling off excess air such as the decompressor thermal technology section assembly of turbine blade and fin usually account for by as described in the 10-18% of logistics of turbine. Therefore, in the VAST circulation, the steam cooling of configuration blade is so that relative air cooling system can reduce 9-15% with the size of compressor.

VAST steam circulation with decompressor surface steam cooling surface intercooler

In improved configuration, the user preferably unites one or more surperficial intercoolers and substitutes steam mixing intercooler, and substitutes the air cooling with the steam cooling. Preferably reclaim the steam of heat from thermal technology's section of decompressor, and return the upstream and enter described burner. This has reduced the cooling of the high-energy fluid (working fluid) of conventional steam cooling. Use this class VAST steam circulation configuration, estimate relatively to have the spraying intercooler and come the VAST steam of cooling turbine machine blade to circulate with compressed air, its efficient can improve about 3-4%. For example, use component efficiency and the parameter of Traverso hypothesis, with respect to 51% efficient of the circulation of not adopting these measures, when 50MW and 1300 ℃, estimate to use the system effectiveness of this class VAST steam circulation configuration to be higher than 54%. That is, to these configurations, cycle efficieny improves 6% approximately.

The diluent supply system

The diluent source

Hot diluent/heating element

Many embodiments are preferably carried fluid water by the direct contact type distributor, cool off reacting fluid and limit the temperature of described high-energy fluid as described hot diluent. For example the colder assembly of electronic building brick can make it keep low temperature with aqueous water. Other for example evaporimeter make water boiling form steam. The used steam of described superheater heating, this steam is used for reclaiming heat from the high-energy fluid that expands.

To the burn carbon dioxide that forms of some embodiment partly recycles as hot diluent or described diluent component and limits ignition temperature.

Conventional fuel-sean is burnt dynamical system and is used excess air as hot diluent. The present embodiment preferably substitutes most of excess air of hot diluent that is used as to improve the thermal efficiency. In some configuration, the user can be with some burning gases or the EGR that leaves described diluent recovery system as diluent, and described waste gas comprises the excessive oxygen of nitrogen, carbon dioxide, water vapour and part.

Some embodiment uses the natural or artificial oil of low evaporation pressure as hot diluent in one or more distributed direct contactors. In some configuration, according to demand or the requirement of various application to the diluent characteristic, can use the synthetic hot fluid such as fluorocarbon.

In certain embodiments, distributed contactor can provide at least a cold (or heat) reactant and/or product to reaction component, and it is mixed to limit (or rising) described temperature. Particularly, some measure is with part waste gas or the circulation of discharging gas, and these gases comprise at least part of carbon dioxide, water vapour, nitrogen and/or relevant inert gas. Product separation and purification system and reactant recirculating system have been simplified in this class measure greatly.

Store system around

In some configuration, the user preferably provides stocking system that fuel flow (for example Diesel#2), hot diluent (for example supply water, process water) or one or more logistics that contain in the oxidant fluid (for example compressed air, oxygen-enriched air and/or oxygen) are cushioned. Described stocking system can comprise storage tank, pipeline, hold the relevant container with other in pond. Be preferably and process or untreated fluid configuration storage tank.

In the clean positive water balance configuration that no sale water is provided, the configuration of the preferred relatively conventional system of user reduces the size of water supplier tank. For example, they provide the water of capacity to start until realize positive water balance, and/or after positive water balance no longer is provided shutdown system. These measures have significantly reduced cost and the trace of water supply system.

Have positive water purification balance and having in the configuration that water sells, the user disposes the size of processing the water supplier tank, to send the interval to cushion in demand peak phase and low ebb phase or water transport. For example in the daytime demand or periodic oil tanker loading.

Pump

When providing the diluent fluid to substitute normally gaseous hot diluent, the user preferably sends into the liquid heat diluent pump heat and the quality transmission system 6000 in the energy conversion system. Referring to, Figure 14 for example. For example, pump into aqueous water and substitute excessive compressed air as hot diluent and/or cooling agent. The user preferably comes the pressurization of described liquid diluent with efficient liquid pump, and it is most of or all be conveyed into the oxidant fluid that contains of described turbine upstream.

The user preferably is pumped at least a portion in the described liquid diluent in one or more recuperation of heat assemblies. For example, one or more in economizer, evaporimeter, superheater and the regenerative apparatus. Then, the diluent after the user will heat is sent into described containing in oxidant fluid stream or the high-energy fluid stream with pipeline, and it is usually located at the upstream of turbine. In some configuration, the user provides hot diluent to described turbine blade, fin and machine wall.

The user preferably disposes the size of liquid diluent pump, diluent is pumped into the position of maximum pressure with maximum volume so that required maximum pressure to be provided. For example, the maximum pressure of the high-energy fluid in the described burner is added the pressure that is enough to overcome the pressure loss between described pump and the described burner than adding superpressure and the differential pressure of diluent conveying by direct fluid contact device.

The diluent treatment system

Hot diluent filters

With reference to Fig. 2 and Figure 15, the user preferably provides fluid treatment system (TRE) 2300 before hot diluent is applied to energy conversion system it to be processed. For example, the user preferably provides filter to come to remove particulate in being pumped into as required the hot diluent the system.

When this VAST circulation is disposed three fluid combustion devices, diluent is spurted into contained oxidant fluid or when directly other of contactor used, such as in ' 191 patent application and the three fluid reactor patent applications instruction ground, need pay special attention to and will from will inject the fluid by distributed direct fluid contact organ pipe road, filter out particulate.

The user preferably processes workshop section at fluid provides the hole large as far as possible filter, and to remove as far as possible the particle greater than required size from diluent (such as water), this size can be blocked the hole of distributed contactor. This particulate is removed measure is benefited system by remove the component (particulate that for example suspends in the water) that may pollute turbine from hot diluent. This has improved average efficiency and the availability of turbine, and has reduced the maintenance and repair expense.

Hot diluent is processed

In order to keep the service life of hot gas path parts, gas turbine manufacturer has stipulated the alloy limit in the hot gas path usually, to keep their warranty period. Also recommended similar value to limit the corrosion of heat passage.

What pay close attention to most is the trace metal alloy, particularly vanadium, sodium, potassium, lead and calcium. These alloys can produce corrosive combustion product. For example, sodium sulphate, sodium vanadate and vanadic anhydride. Usually every kind of potential dopant source-air, water and fuel have all been stipulated the limit (usually in the 0.5-2ppm scope) of these metals.

Use conventional air filtration and suitable operation so that intake air or transpirable cooling agent have minimum carry over (carryover), air-source less and except in harsh environment all in the concentration of defined limits. Gas source on the conventional market does not find to contain these trace elements of the amount that should be noted. Therefore, use filtered air and natural gas, circulation does not need to consider this class alloy usually to VAST.

The liquid fuel in great majority source contains the enough high-caliber alloy of paying close attention to, particularly vanadium really. Therefore, generally include for the liquid fuel processing procedure that trace element is reduced to predeterminated level, to help satisfying these dopant levels, whether no matter the recovery and reuse of diluent arranged. To the circulation such as STIG and HAT circulation of diluent consumption more than yield, need to process continuously the diluent of supplementing water and recovery.

Diluent in the VAST circulation is processed

In most of VAST circulation, diluent is put and operated to reclaim in described system with apolegamy, and its amount is more than the described oxidant that is conveyed into decompressor 5100 outlet upstreams and the dilution dosage in the high-energy fluid. Under most conditions, this has eliminated the demand to supplementing water. The VAST required water of recyclable unnecessary recirculation that circulates produces supplementing water and replenishes other water loss. (when the water loss in the heat that leakage is being arranged is used surpasses the water recovery ability of VAST circulation, may need a certain amount of supplementing water).

The clean fuel of use such as natural gas and the good input air of filtration do not need the diluent of recovery and reuse is further processed (referring to table 6) in conventional VAST circulation. This conclusion is the alloy limit of announcing using a gas turbine manufacturer, and the gas passage alloy of supposing all sources is accumulated to (the very conservative hypothesis) of making on the basis in the diluent of recovery at last. Be used for estimating that the general formula of described flow is:

             (A/F)X _a+(W/F)X _w+X _fThe limit of＜table 1

X wherein_a、X _w、X _fBe to be respectively to the restriction of the alloy of air, water and fuel, and W is current that inject and A, F are air and fuel flow.

The result shows the use natural gas, can produce the excess amount of diluent of capacity and it is reclaimed by burning, thereby make the concentration of dopant of input obtain enough dilutions, thereby be no more than the gas passage pollutant limit of recommendation. Therefore, in certain embodiments, except controlling the concentration by excessive water discharging or " emptying ", do not need other diluent processing procedure to reduce alloy.

Table 6 uses the VAST-W circulating water treatment of surface condenser
							Air stream (A)	41.6	kg/s
Fuel (F)	2.199	kg/s
							The water (W) that injects	15.33	kg/s
Recirculated water	17.88	kg/s
							Air concentration restriction Xa	5	ppb	Suppose according to GEK 101944, GEI-41047
VAST A/F ratio	18.92		Be lower than GE supposition@50
							＝(A/F+1)/51＝	0.391		2.A/F is not equal to 50 correction factor to the GEK101944 table
Trace metal Xf=	0	Supposing in the air does not have; The trace metal restriction is applied to liquid fuel
							Ca Xf＝	0	Supposing in the air does not have; The trace metal restriction is applied to liquid fuel
							Composition	Restriction*   ppb	Xw limits ppb	Xa   ppb	Total amount ppb	The water ppb that reclaims	Remarks
Na+K	1000	42.5	5.0	859	48.0
							Pb	1000	42.5	5.0	859	48.0
V	500	14.4	5.0	429	24.0	V is not present in air
							Ca	2000	98.5	5.0	1718	96.1
*GEK 101944 tables 2
＝(A/F+1)/51＝	1.00	Be made as 1; Not to GEK101944 table 2, A/F is not equal to 50 correction factor
							Trace metal Xf=	0	Supposing in the air does not have; The trace metal restriction is applied to liquid fuel
Ca Xf＝	0	Supposing in the air does not have; The trace metal restriction is applied to liquid fuel
Composition	Restriction*   ppb	Xw limits ppb	Xa   ppb	Total amount ppb	Condensate ppb	Remarks
							Na+K	1000	130	5.0	2199.0	123.0
Pb	1000	130	5.0	2199.0	123.0
							V	500	58	5.0	1099.5	61.5	V is not present in air
Ca	2000	273	5.0	4398.0	246.0
							*GEK 101944 tables 2

When the liquid fuel (or fuel gas) that uses with capacity alloy (referring to table 7), maybe when having highly doped input air condition, need to process the diluent that reclaims logistics is reduced to desired level. Mixedbed demineralizer can be used as the optional treating apparatus of removing alloy. Because dopant levels is lower, correspondingly regeneration rate is also lower.

Table 7 uses the VAST-W circulating water treatment of surface condenser-liquid fuel
									Be converted into low HV liquid fuel
Air stream (A)	41.6	kg/s	F gas	LHV gas kJ/kg		HV liquid kJ/kg
									Liquid fuel (F)	2.29	kg/s	2.20	44，237.44		42，498.05
The water (W) that injects	15.33	kg/s				1kcal＝4.187kJ
									The water that reclaims	17.88	kg/s
Air concentration restriction Xa	5	ppb	Suppose according to GEK 101944
VAST A/F	18.9		Suppose far below GE
									＝(A/F+1)/51	0.39		To GEK 101944 tables 2, A/F is not equal to 50 correction factor
Total Xw	500	ppb	According to Figure 22, GER3428
									Trace metal Xf	1000	ppb	According to Figure 22, GEK3428
Ca Xf	10000	ppb	According to Figure 22, GER3429
Composition	Restriction ppb	Xf limits ppb	Xa     gpb		Xw     ppb	Condensate ppb
									Na+K	1000	299	5.0		0.05	50.0
Pb	1000	299	5.0		0.05	50.0
									V	500	104	5.0		0.05	025.0
Ca	10000	3814	5.0		0.05	500.0
									*GEK 101944, table 2; GER 3428 tables 22
									(A/F+1)/51＝	1.00	Be made as 1, unmatchful GEK 101944 tables 2, A/F is not equal to 50 correction factor
Composition	Restriction*     ppb	Xf limits ppb	Xa     ppb		Xw     ppb	Condensate ppb
									Na+K	1000	909	5.0		0.05	128.0
Pb	1000	909	5.0		0.05	128.0
									V	0500	409	5.0		0.05	64.0
Ca	10000	9909	5.0		0.05	1280.2
									*GEK 101944, table 2; GER 3428 tables 22

In certain embodiments, the user more preferably provides " effluent (side-stream) " to process, with processing section diluent only but be enough to controlled doping thing level. This has the advantage that reduces the pumping merit, and this will need to not push treatment system with all diluents in addition. The excess amount of diluent discharging adds that the effluent processing can preferably reduce the diluent disposal cost.

In some configuration, larger when sending into the pollutant flow (or concentration) of decompressor by the hot diluent of recirculation, and in the time of can reducing the expense of life cycle by reducing this concentration, maybe when needs reduce alloy flow (concentration), preferably in treatment system 2300, diluent is further processed, to reduce those alloys.

Similarly, when needs or when requiring treated water, the preferred excess amount of diluent stream that forms of processing is to be reduced to necessary or required level with these concentration. Under certain conditions, can with excessive water purifying and the sale of gained, make the water treatment process become revenue source by consumption process.

Can use the water treatment mode such as mixedbed demineralizer. When electrochemical conditions is fit to, also can adopt other processing method such as the demineraliting agent of counter-infiltration and other type. The inconsistent chemical substance of assembly that these processing methods have been removed and it be about to inject, described assembly is turbine heat passage assembly for example, can comprise one or more in turbine blade, turbine fin and the guard shield.

The user preferably comes the diluent of filter freezing by one or more filters, to reduce described particulate load capacity. The preferred filter with homogeneous aperture that uses, this aperture be less than the hole in the distributed contactor, thereby prevent that the diluent particulate is infected with these holes.

Can use the gross porosity filter of amphistyly, thereby when can other filter in described twin installation still working, clean online or replace filter media. In embodiments, can use little automatic back flush filtration medium filter to 100 microns.

Can filter greater than about 10 microns particulate with fine filter in certain embodiments. These filters can comprise such as the grains of sand and anthracitic medium filter.

In some configuration, the user preferably before carrying out follow-up pH processing, reduces the CO2 concentration in the diluent condensate. The user preferably provides the recompression machine, and as required or require to make the pressure behind the condenser to be brought down below ambient pressure, to reduce the carbon dioxide in the diluent and/or to improve the thermoeconomics of system. In some configuration, the recompression machine that VAST circulation is provided has removed enough carbon dioxide in itself inside.

Utilize the hot diluent dissolving of condensation and reclaim the sour gas of some formation. For example, nitrogen dioxide, sulfur dioxide and carbon dioxide of part etc. Compare with the prior art of routine, can significantly reduce nitrogen oxide and the carbon monoxide (NOx and CO) that forms in the combustion process to temperature controlled reinforcement in the VAST cyclic burner, and be similar to the level of catalytic combustion.

Provide clean positive water balance in VAST circulation configuration, the concentration of these acidic components alloys can reach and the water yield proportional balance of growing amount divided by discharging. Preferred configuration-system has enough acid resistances when assembly is operated under these acidic components concentration.

In the acid system that processes of needs, the user preferably provides the amberplex of required size or similar acid treatment system to process described acid logistics. Because the alloy amount that forms is lower, and partly discharges with the excessive water that forms, therefore estimate that the size of described recirculation diluent treatment system is significantly less than conventional system and more cheap.

Corresponding to less processing demands and less treatment facility, the expense that the expectation user processes and recycles condensate is starkly lower than " wetting " circulation of conventional prior art. In the great majority configuration, all outside supplementing water demands have almost been eliminated.

Combustion system

The combustion chamber

With reference to Figure 21, and for preferred VAST burner and temperature control method are described, referring to ' 191 patent application and three fluid patent applications.

Burner outlet/turbine inlet temperature

With reference to Fig. 1, the user preferably uses diluent induction system 2000 to provide the diluent of processing to described burner, with the temperature of control high-energy fluid. Before it is delivered to described burner, preferably in heat and quality transmission system, uses this diluent and come cooling package and from hot converting system, reclaim heat. It is reported that when the temperature of high-energy fluid reduces or the about 10K (18 °F) that raises, then the life-span of turbine blade is double or reduce by half. Yet, during to about 1300 ℃ typical turbine inlet temperature, the uncertainty that temperature of the prior art detects for approximately+/-10K. The preferred burner with operating the numerical value of controlling more accurately burner outlet or turbine inlet temperature (TIT) of VAST circulation.

The user preferably controls the fluid of burner configuration pinpoint accuracy, particularly to the diluent fluid. Preferred configuration Ginter VAST burner, or more preferably dispose the three fluid VAST burners of instructing as in three fluid patent applications and ' 191 patent application.

For example, preferably use disclosed VAST three fluid combustion devices in the three fluid patent applications, coming provides more accurately control to containing fuel fluid and containing the diluent fluid, especially when they are liquid state. Similarly, when working under near stoichiometric condition, the VAST burner is controlled oxidant to the ratio of fuel more accurately by the concentration of monitoring remaining oxidant.

As herein with other places as described in, the user preferably disposes described burner and controls described hot diluent flow, so that one or more following advantages to be provided:

Turbine inlet temperature numerical value

Reduce uncertainty

Turbine inlet temperature distributes

Reduce and distribute/" distribution factor (profile factor) "

Reduce or eliminate bushing pipe (liner) cooling

The uncertainty that temperature distributes when reducing higher mean temperature

Reduce the cross direction profiles of temperature uncertainty

By this preferred burner that provides and fluid control measure, the fluid flow that the user can obtain to significantly improve is controlled, thereby improves the uncertainty in the control of high-energy fluid temperature. More particularly, described three fluid combustion devices have been controlled the cross direction profiles that fluid is carried. Therefore, the user can dispose and control the transverse temperature distribution in the high-energy fluid. This so that the uncertainty when the control numerical value of described high-energy fluid peak temperature and position improve. Described three fluid combustion devices have further improved the control of the erratical fluctuations of fluid flow, and then have improved the control to the erratical fluctuations of high-energy fluid temperature. These features have reduced simultaneously temperature and have been controlled at uncertainty on the room and time. It has also realized passing through the cross direction profiles of the uncertainty of described high-energy fluid.

Higher transverse temperature distributes

The user preferably is controlled at the spatial peaks temperature of high-energy fluid in required probable range and is less than or equal to required peak temperature. According to the required probability that is no more than this temperature, required peak temperature preferably is defined as the standard deviation that the required peak temperature of decompressor thermal technology section assembly deducts spatial peaks temperature in one or more high-energy fluids.

In similar pattern, the user preferably disposes and is controlled to be the value that the temperature cross direction profiles required with entering decompressor has skew with the transverse temperature distribution of high-energy fluid. The temperature that for example strides across turbine blade from the center to the tip distributes. The multiply each other value of gained of the local uncertainty in space that the cross direction profiles that the temperature cross direction profiles of high-energy fluid further preferably is set to required decompressor inlet temperature deducts required multiplication factor and temperature uncertainty cross direction profiles.

By realizing lower uncertainty spatial distribution at whole decompressor entrance, the high-energy fluid that enters described decompressor can have the tolerant temperature cross direction profiles of being permitted scope. By this higher temperature cross direction profiles, compare the prior art in temperature space and the larger uncertainty of time control existence, the user can obtain higher high-energy fluid mean temperature. In energy conversion system, this higher mean temperature has been given higher thermodynamic efficiency.

The burner cooling system

The preferred assembly that at first comes heat of cooling sensitivity with the cold cooling fluid to temperature. With reference to Figure 19, preferably in heat and quality system 6000, come the assembly absorbing heat that is heated from heat-sensing with surface heat exchanger. For example, such as in the three fluid patent applications instruction ground, preferably with pipeline cooling agent is carried through the pressure vessel around described combustion chamber. In order to help to reclaim heat, configurable heat-insulation layer is to reduce to the heat loss of external environment. For example, as shown in figure 19, center on the burner cooling system with heat-insulation layer. The user preferably designs the pressure vessel cooling system, remains on the temperature with pressure vessel to be lower than about 533K (about 260 ℃ or 500 °F), thereby uses the cheap pressure vessel assembly that meets general ASME standard.

Then, the user preferably is conveyed into combustion chamber 4100 with the water after heating as hot diluent with direct fluid contact device. This has significantly reduced the heat loss of described burner.

Such as institute's instruction in three fluid reactor patent applications and ' 191 patent application, the user preferably disposes burning wall or " bushing pipe (liner) ", the affined combustion process of carrying out under near the stoichiometric(al) combustion condition that it can process that described VAST circulation provides and the hot diluent cooling procedure of adding. As shown in figure 21, but user's additional configuration bushing pipe cooling system further cools off this burner bushing pipe, and reclaims this senior heat. The diluent F275 of oxidant fluid F160, fuel F320, liquid diluent F276 and vaporization is provided to described burner usually, and fuel combustion also produces high-energy fluid F405. With pipeline the lower temperature fluid is sent into cooling system around described cooler, to control as required wall temperature. These cryogens become hotter fluid and are recovered, for example superheated steam. The hot diluent that preferably will so heat at the burning wall is transported to the upstream of burner to provide more uniform temperature to distribute.

The user preferably eliminates the excessive oxidant fluid that contains of conveying, and burner bushing pipe wall (for example, compressed air and/or steam) is passed through in its conveying as hot diluent or cooling agent. This makes it possible to improve the temperature distribution of whole burner, and high energy gas can be by this class bushing pipe heat of cooling diluent cooling. (that is, more the temperature of homogeneous distributes, or " distribution factor (profile factor) " is more near homogeneous). Improve described " distribution factor " and then improved the thermal efficiency of system.

In the improved configuration, the user in some configuration as required or require to provide hot diluent to cool off described burner bushing pipe wall. The further details of this class burner cooling system is referring to three fluid patent applications (especially with reference to Figure 28 and Figure 30) and ' 191 patent application. Described burner bushing pipe is preferably placed in the pressure vessel, thereby the pressure of described bushing pipe cooling agent only needs enough diluent to be carried by this bushing pipe. For example, can adopt the cooling agent carrier pipe of liner (lined) with the protection high-temperature metal to steam. Perhaps can adopt refractory ceramics. In certain embodiments, in combustion system configurable radiation shield to remove heat and keeping system cooling from described combustion system.

When requiring or need, in some configuration, the method user of similar cooling burner bushing pipe preferably provides hot diluent to cool off the wall of burner-turbine transitional region. Preferably the diluent of consequent heat is sent into burner through the upstream providing more uniform temperature to distribute, and reclaimed these heats and do not dilute and cool off high-energy fluid.

Fuel delivery system

The fuel source

Fluid fuel, diluent/heater

VAST circulation embodiment preferably adopts the embodiment of the three at least a fluid combustion devices in the fuel that can use numerous fluid fuels or fluidisation of instructing in three following fluid patent applications and ' 191 patent application. Some embodiment preferably provides the pluralities of fuel configuration, and these fuel namely have also gaseous state of liquid state. For example, natural gas and diesel fuel. This has reduced fuel price fluctuation and the unstable economic risk that causes of originating. Other configuration can be used multiple liquid fuel. Use liquid fuel three fluid combustion devices can improve the dynamic property liquid fuel.

Some embodiment configuration is used for mixing pluralities of fuel, reduce and carry relevant expense, and the fuel of different calorific values mixed to reduce fuel, conveying and carrying cost, fuel disposal cost and alleviate one or more parameter costs in the expense of this class impact (such as polymerization).

Optionally come to provide logistics and required pressure (referring to Figure 26) to combustion system as required with pump, compressor and control valve. (note, enough when the supply pressure of external fuel in some cases, for example from pipeline or storage tank, can reduce or remove some pump or compressor. )

The fuel type

Certain embodiments of the present invention can adopt one or more in numerous liquid fuels. For example:

Petroleum liquid fuel and distillate (distillate) fuel comprises aviation fuel, gasoline, kerosene, diesel fuel, fuel oil, bunker oil, crude oil, tar sand (tar sand) oil, shale oil, heavy fossil liquid, coal derive fuel, and liquefied natural gas (LNG);

Vegetable oil comprises palm oil, coconut oil, soya-bean oil, bird rape seed oil, rapeseed oil (canola oil) and peanut oil;

The ester of this class vegetable oil;

The cracking fuel that obtains by heating living beings or fossil hydrocarbon;

Oxygenated fuel comprises methyl alcohol, ethanol and MTBE;

Without the charcoal liquid fuel, comprise liquified hydrogen, liquefied ammonia.

Certain embodiments of the present invention can adopt one or more in numerous fuel gas. For example:

Most fossil bases or petroleum base gas comprise natural gas, coal bed (coal bed) methane, propane and butane;

By producer gas or the forming gas that the fossil fuel that comprises coal, tar sand and heavy fuel is gasified and generates with air, oxygen-enriched air or oxygen, methane and other hydrocarbon part of comprising carbon monoxide and hydrogen and the non-quantitative of non-quantitative, and comprise arbitrarily and fuel and/or the diluent of remaining reaction comprise nitrogen and carbon dioxide;

In air, oxygen-enriched air or oxygen to living beings gasify producer gas or the forming gas of gained;

Hydrogen or other are without charcoal fuel etc.;

The gas that biogas or other living beings discharge.

Aqueous fuel

Some embodiment provides the fluid that contains one or more described fuel water. For example:

Be dissolved with the oxygenated fuel such as ethanol and methyl alcohol of water;

Fuel-aqueous emulsion comprises the water with any above-mentioned liquid fuel emulsification, optional emulsifying agent or surfactant, for example " Orimulsion of comprising^”；

The water that mixes with fuel comprises in the fuel containing the fuel drop in the free of water droplets and water;

The fuel gas that mixes with water smoke, steam or steam;

The mixture of above-mentioned fuel.

The solid fuel that suspends

Some embodiment preferably suspends, carries secretly or the solid fuel particle of fluidisation with containing oxidant fluid. For example:

In air or fluid fuel, carry secretly or any coal fine powder of fluidisation, comprise brown coal powder, bituminous coal powder, anthracite powder.

In air or fluid fuel, carry secretly or any living beings fine powder of fluidisation, comprise grain component of sawdust, timber powder, active carbon powder, flour, rice husk, pulverizing etc.

The fuel treatment system

With reference to Fig. 4, the user preferably provides fuel processing installation to come fuel is processed and modulate to be used for energy conversion system.

Fuel filters

Described in ' 191 patent application and three fluid patent applications, the user preferably provides filter to remove particulate in the fluid fuel of supplying. Preferably provide the aperture large as far as possible filter, it blocks the particulate in distributed contactor hole with required probability except deenergizing. For example hole dimension is about 2/3 uniform filter of the direct contactor hole dimension of porous. This particulate removal device is benefited system by the fuel element of removing the turbine that can mix. This has improved turbine average efficiency and availability, and has reduced the maintenance and repair expense. Can wash with desalination fuel.

In improved embodiment, the user can heat to improve performance to described fuel. Liquid towards fuel is preheated to selected temperature range and can reduces the illeffects such as polymerization and coking. To fuel gas, heating can be eliminated the moisture of carrying secretly, and these moistures can endanger described fuel-induction system or combustion system assembly. Can heat by following one or more logistics: the diluent fluid of the oxidant fluid of high-energy fluid, expansion fluid, compression, heat or the cooling agent fluid of heat. The assembly that available inside is heated for example generator heats fuel.

Expansion system

Turbine

Turbine expansion ratio (expansion ratio)

When the needs mechanical or electrical energy, the user preferably is sent to decompressor with high-energy fluid, and makes high-energy fluid be expanded to lower pressure from elevated pressures. The part of the mechanical energy that produces can be used for driving generator, subsequently described expansion fluid be disposed to diffuser (diffuser) (or chimney). (referring to, Figure 23 for example).

In relatively large system, as shown in figure 24, high-energy fluid is expanded expand by a plurality of expansion workshop section of series winding.

With reference to Figure 20, the diluent of preferably being carried by heat and quality transmission system 6000 cools off the one or more hot assembly in the decompressor expansion workshop section. For example the turbine fin of one or more workshop sections, turbine blade, turbine wheel cap and turbine hub (hub).

With reference to Fig. 8 and Figure 25, in certain embodiments, the user is preferably with the one or more compressors before the burner and the combination of the recompression machine behind decompressor and the condenser. By so, can obtain clean expansion ratio (β_Turbine), this clean expansion ratio is the one or more compressor pressure ratio (β before the described turbine_lpc，β _hpc) multiply by the pressure ratio (β of recompression machine_rec), deduct again the result that the pressure loss effect between entrance and exit obtains. By this method, can obtain clean turbine expansion ratio apparently higher than the conventional pressure ratio between burner and the external environment.

By being equipped with the recompression machine to VAST-WS circulation, total turbine expansion ratio preferably is configured to integrated oxidation agent compression ratio β, and to be about 10 o'clock overall expansion ratios be that 37 to oxidant compression ratio β to be about 44 o'clock overall expansion ratios be 102.8 scope. Therefore, being added in of machine of recompression significantly improved total turbine expansion ratio under the condition of not using the super-pressure assembly. It is also so that can compress at a lower temperature.

This total turbine expansion ratio roughly changes along with required entrance oxidant compression ratio. More preferably, it is recompression in about 10 o'clock than for about 3.7 that described recompression ratio is configured to compression ratio, to compression ratio be recompression in about 44 o'clock than being about 2.3 scope.

The user preferably disposes described total turbine expansion ratio (β turbine), obtains performance required or that improve to help VAST steam circulation (VAST-WS). Table 8, table 9 and table 10 have shown that the total oxidant compression ratio is about the configuration (collocation method is shown in table 11 and Figure 51) of 30 VAST water circulation (VAST-W). More preferably described VAST-W circulation is adjusted to about 60 pressure ratio (referring to table 12, table 13 and table 14), provide configuration near best economic profit rate with the industrial turbines of giving about 50MW, wherein adopt American industry usefulness gas and electricity consumption average price in 2000, and suppose that parameter such as Traverso and Massardo are selected to contrast other wet circulation. It is about 1.71 that the pressure ratio that preferably recompresses machine is set to, to obtain about 102.5 the clean turbine expansion ratio of associating.

The table 8 pair device parameter that VAST-water circulation (VAST-W) (30) is supposed and calculated
									For example, to 50MW, TIT=1300EC, β=30
Parts	Sign	Specify			Calculate
											Polytropic efficiency (Poly.Eff.)	T. press from both sides a little	Other	Constant enthalpy efficient (Isen.Eff.)	Validity	Surface area	The Q that shifts
			EC				m2	kW
									1310	LPC	0.924			0.9144
1700	LGC			Saturation degree=100%
									1350	HPC	0.924			0.8947
4100	CBC			Excess air=1.05
									5100	EXP	0.8607		Mech.Eff.=0.98 decompressor cooling agent/total flow=0.1128	0.9121
6500	ECO			Be up to and be lower than 3 ℃ of boiling temperatures		0.9668	5,827	18,265
									7400	FGC		5	Saturation degree=100%		0.9401	2,116	42,975
5300	RCP	0.924			0.9102
									5200	GEN			Electrical efficiency=0.985
7100	HX *					0.9128	161	522
									7600	COL		10			0.72	2720	41206
	All pumps		Hydraulic efficiency=0.83; Mechanical efficiency=0.90
									*This adds ordinary circumstance, but can remove in this configuration

Table 9 logistics forms: VAST-water circulation (VAST-W) (30)
									For example, to 50MW, TIT=1300EC, β=30. The numerical value that italic represents is assumed value
Occur for the first time (Occurrence)		CH4	H2O(L)	H2O(V)	N2	CO2	O2	Logistics
									Input air	Molar fraction			0.01	0.782	0	0.207	100，101，1   02
Mass fraction			0.006	0.762	0.001	0.231
								Behind the intercooler		Molar fraction			0.052	0.749	0	0.199	103，160，1   70
Mass fraction			0.033	0.742	0.001	0.225
									Fuel	Molar fraction	0.93			0.07			320
Mass fraction	0.884			0.116
								Behind the burner		Molar fraction			0.48	0.457	0.057	0.006	405
Mass fraction			0.358	0.53	0.105	0.008
									Behind the decompressor				Non-availability				420，430
Behind the surface condenser	Molar fraction			0.148	0.736	0.079	0.037	460，421，4   75
									Mass fraction			0.095	0.738	0.124	0.043
	Dew-point temperature=53.95 ℃.
									Other logistics is pure liquid H2O

Table 10 logistics numerical value: VAST-water circulation (VAST-W) (30)
																				For example, to 50MW, TIT=1300 ℃, β=30. The numerical value that runic represents is assumed value
Unit	Title	Logistics	Mass flow Kg/s	Temperature EC	The pressure bar	PwrMe   MW	PwrEI   MW	ΔP	ΔQ	Unit	Title	Logistics	Mass flow kg/s	Temperature EC	The pressure bar	PwrMe  MW	PwrEl   MW	ΔP	ΔQ
																				The input logistics
1100	OXS	100	42.51	15	1.01
																				2100	DIS	200	0	15	3
3100	FUS	320	2.25	25	41.88
																				*1200	TRE	100	42.51	15	1.01					7100	HX	421	44.25	167.5	1.03
		101	42.51	15	1			1％				475	44.25	156.9	1.02			2％
																				1310	LPC	101	42.51	15	1							247	0.25	70.93	100
		102	42.51	101.8	2.36							270	1.17	157.5	97			4％	1％
																						500	0	0	0	-4				5900	STA	475	44.25	156.9	1.02
1700	LGC	102	42.51	101.8	2.36								44.25	156.9	1.01			1％
																						270	1.17	157.5	97					7600	COL	242	378.3	51.08	3
		103	43.68	49.8	2.36				1％			243	378.3	25.01	2.88			4％
																				1350	HPC	103	43.68	49.8	2.36						PUM	CWIN	374.5	15	1.01
		160	37.03	415.4	29.91							CWINP	374.5	15.01	2		-0.05
																						170	6.65	415.4	29.91							CWOUT	374.5	41.08	1.92			4％
		501	0	0	0	-17				7820	PUM	246	378.3	51.08	2.77
																				4100	CBC	160	37.03	415.4	29.91							242	378.3	51.08	3		-0.009
		320	2.25	25	41.88					6100	MIX	241	363.5	51.93	2.77
																						230	13.05	344.4	160							245	14.73	30.02	3
		405	52.32	1300	29.01			3％	1％			246	378.3	51.08	2.77
																				5100	EXP	405	52.32	1300	29.01					7810	PUM	244	14.73	30	0.29
		170	6.65	415.4	29.91							245	14.73	30.02	3		-0.005
																						420	58.98	354.4	0.29					6300	SPL	240	378.3	51.93	2.77
		580	0	0	0	80						295	14.73	51.93	2.77
																				6500	ECO	420	58.98	354.4	0.29							241	363.5	51.93	2.77

Table 10 logistics numerical value: VAST-water circulation (VAST-W) (30)
																				For example, to 50MW, TIT=1300 ℃, β=30. The numerical value that runic represents is assumed value
Unit	Title	Logistics	Mass flow Kg/s	Temperature EC	The pressure bar	PwrMe   MW	PwrEl   MW	ΔP	ΔQ	Unit	Title	Logistics	Mass flow kg/s	Temperature EC	The pressure bar	PwrMe   MW	PwrEl   MW	ΔP	ΔQ
																						430	58.98	124	0.29			2％		2300	TRE	295	14.73	51.93	2.77
		249	13.05	53.35	165							201	14.22	51.93	2.65			4％
																						230	13.05	344.4	160			4％	1％	2100	DIS	200	0	15	3
7400	FGC	430	58.98	124	0.29					8500	DWD	290	0.51	51.93	2.77
																						460	44.25	30	0.29			2％		2200	PUM	201	14.22	51.93	2.65
		243	378.3	25.01	2.88							220	14.22	52.78	100		-0.184
																						240	378.3	51.93	2.77			4％		6320	SPL	220	14.22	52.78	100
		244	14.73	30	0.29				1％			248	13.05	52.78	100
																				5300	RCP	460	44.25	30	0.29							247	1.17	52.78	100
		421	44.25	167.5	1.03					7800	PUM	248	13.05	52.78	100
																						531	0	0	0	-7						249	1.17	52.78	100		-0.112
5200	GEN	530				52	50		-	Clean electricity output							50

Table 11 is used for the computational methods of VAST-W (β=30) and VAST-W (β=60)
1	Set fixed variable: (numerical value of demonstration is for being used for the numerical value of this actual configuration. )
		T(F100)＝15℃.			P(F100)＝1.01bar		X (F100)=[referring to forming explanation]
												T(F200)＝15℃.			P (F200)=3 bar
		T(F320)＝25℃.			To β=30: P (F320)=41.88 bar
															To β=60: P (F320)=83.96 bar
		X (F320)=[referring to forming explanation]
		The pressure drop of all devices (Δ P) and heat loss (Δ Q) are presented in the logistics numerical tabular
												The cold Δ T=3 of mistake among the F275 ℃.
												T (cooling water)=15 ℃.
		Temperature in 7600 (COL) folder point=10 ℃.
		Polytropic efficiency 1310 (LPC)=0.9240
												Polytropic efficiency 1350 (HPC)=0.9240
		Polytropic efficiency 5100 (EXP)=0.8607
												Polytropic efficiency 5300 (RCP)=0.9240
												P (F275)=160 bar
		T (F275) is excessively cold=and 3 ℃.
		Logistics F103 is saturated with H2O
		Actual O2 is to stoichiometric ratio=1.05
												T(F405)＝1300℃.
												Total flow in blade cooling agent/decompressor=0.1067
		The mechanical efficiency of decompressor 5100 (EXP)=0.98
		Temperature among 7400 (FGC) folder point=5 ℃.
												Steam F460 (leaving the gas logistics of FGC) is saturated.
												The electrical efficiency of generator 5200 (GEN)=0.985
		The hydraulic efficiency of all pumps=0.83
											The mechanical efficiency of all pumps=0.9
												To β=30: T (F475)=156.90
		To β=60: T (F475)=82.55

Table 11 is used for the computational methods of VAST-W (β=30) and VAST-W (β=60)
												To β=30; The pressure ratio of getting two compressors is 30
										2	Primary Calculation
	Calculate 1200 (TRE) to obtain X (F101), P (F101) and T (F101)
									Calculate T (F275) based on crossing cold numerical value
	Temperature folder point among T (F24)=T (cooling water)+7600 (COL)
									3	Initial designs variable: (showing numerical value=selected numerical value)
	To β=30: P (F102)=2.36 bar							P (F420)=0.29 bar
										To β=60: P (F102)=1.22 bar					P (F160)=59.97 bar		P (F420)=0.62 bar
		4	Calculate the pressure of all logistics from pressure, Δ P ' s and the described design variable of hypothesis
											5	Suppose that base value is F101=1kg/s, and calculate 1310 (LPC) to obtain W500, F102 and T (F102) based on X (F101).
		6	Conjecture T (F270) (final value after the iteration)						To β=30: T (F270)=157.50
To β=60: T (F270)=72.59 ℃ .)
											(note: because the numerical value of F270 is less, described calculating is not very responsive to this value)
		7	Suppose that logistics F103 is saturated, and calculate 1700 (LGC) with acquisition F270, F103, | X (F103) and T (F103).
												8	Calculate 1350 (HPC) to obtain F160, T (F160), W501 and T (F170)
		9	Suppose that base value is F320=1kg/s fuel. Based on X (F320), excessive 02 ratio of supposing and T (F405)
													Calculate 4100 (CBC) to obtain actual F160, F405, X (F405)
		10	According to the ratio of blade cooling agent to the total flow by decompressor, calculate F170
												11	According to the summation of F160 and F170, adjust F103, F102, F270, F101.F100=F101
		12	According to given polytropic efficiency, calculate 5100 (EXP) to obtain F420 and T (F420).
												13	Conjecture T (F248) (final value after the iteration)					To β=30: T (F248)=52.78
To β=60: T (F248)=70.93 ℃ .)
					14	Calculate 7800 (PUM) to obtain F249, T (F249)
													15	Calculate 6500 (ECO) to obtain F430, T (F430)
					16	Press from both sides point according to saturated logistics F460 with to the temperature of 7400 (FGC), calculate 7400 to obtain T (F460), F460, X (F460), F244, F240, T (F240), F246, T (F246).
													17	Get F295=F246 and calculate 6300 to obtain T (F295), F241, T (F241)
					18	Get F201=F249+F270.
													19	Calculate 2300 (TRE) to obtain F200 or (F290 and T (F290))
					20	Calculate 2200 (PUM) to obtain F220, T (F220)

Table 11 is used for the computational methods of VAST-W (β=30) and VAST-W (β=60)
								21	Calculate 6320 (SPL) to obtain T (F248), F255, T (F255)
		22	Does T (F248) meet the T (F248) of hypothesis in the step 13? if not, adjust T (F248) and begin to compute repeatedly from step 13. If so, continue.
							23	According to its polytropic efficiency, calculate 5300 (RCP) to obtain F241 and T (F241)
		24	According to the T475 of appointment or to the explanation of the number of degrees that are higher than saturation degree, calculate T475 and Q (7100)
							25	Calculate HX (7100) to obtain F270 and T (F270)
	26	Does T (F270) meet the T (F270) of hypothesis in step 6? if not, adjust T (F270) and begin to compute repeatedly from step 6. If so, continue.
						27	Calculate 6100 (MIX) to obtain F242, T (F242)
	28	Calculate 7820 (PUM) to obtain F243, T (F243)
						29	Calculate 7600 (COL)
	30	Calculate all heat transmitter areas.
						31	Calculate all capital costs and Master Cost and generating quantity.

Table 12 hypothesis and the device parameter that calculates: VAST water circulation (YAST-W) (60)
									For example, to β=60, TIT=1300EC (～Opt IRR)
Sequence number	Sign	Designated value			Calculated value
											Polytropic efficiency	T presss from both sides point	Other	Constant enthalpy efficient	Validity	Surface area	The Q that shifts
			EC				m2	kW
									1310	LPC	0.924			0.9219
1700	LGC			Saturation degree=100%
									1350	EPC	0.924			0.8779
4100	CBC			λA/F rel＝1.05
									5100	EXP	0.8607		Mechanical efficiency=0.98 decompressor cooling agent/total flow=0.1067	0.9114
6500	ECO			Maximum temperature is made as and is lower than boiling point 3EC		0.9013	5,469	21,224
									7400	FGC		5	Saturation degree=100%		0.9380	3,400	53,738
5300	RCP	0.924			0.9183
									5200	GEN			Electrical efficiency=0.985
7100	HX *					0.1418	1.92	1.66
									7600	COL		10
	All pumps		Hydraulic efficiency=0.83; Mechanical efficiency=0.90
									*This adds ordinary circumstance, but can remove in this configuration.

Table 13 logistics forms: VAST-water circulation (VAST-W) (60)
									For example, to β=60, TIT=1300EC (～Opt IRR)
Occur for the first time		CH4	H2O(L)	H2O(V)	N2	CO2	O2	Logistics
									Input air	Molar fraction			0.01	0.782	0	0.207	100，101，102
Mass fraction			0.006	0.762	0.007	0.231
								In ask cooler after		Molar fraction			0.019	0.775	0	0.206	103，160，170
Mass fraction			0.012	0.758	0.001	0.23
									Fuel	Molar fraction	0.93			0.07			320
Mass fraction	0.884			0.116
								Behind the burner		Molar fraction			0.508	0.432	0.054	0.005	405
Mass fraction			0.384	0.508	0.1	0.007
									Behind the decompressor				Non-availability				420，430
Behind the surface condenser	Molar fraction			0.07	0.803	0.086	0.041	460，421，475
									Mass fraction			0.044	0.78	0.131	0.045
	Dew-point temperature=39.36 ℃.
									All other logistics are pure liquid H2O

Table 14 logistics numerical value: VAST-water circulation (VAST-W) (60)
																				For example, to β=60, TIT=1300 ℃ (～Opt.IRR). The numerical value that runic represents is assumed value
Unit	Title	Logistics	Mass flow kg/s	Temperature EC	The pressure bar	PwrMe   MW	PwrEl   MW	ΔP	ΔQ	Unit	Title	Logistics	Mass flow kg/s	Temperature EC	The pressure bar	PwrMe  MW	PwrEl   MW	ΔP	ΔQ
																				The input logistics
1100	OXS	100	42.39	15	1.01
																				2100	DIS	200	0	15	3
3100	FUS	320	2.24	25	83.96
																				Equipment and logistics
1200	TRE	100	42.39	15	1.01					7100	HX	421	41.76	82.59	1.03
																						101	42.39	15	1			1％				475	41.76	82.55	1.02			2％
1310	LPC	101	42.39	15	1							247	0.25	70.93	100
																						102	42.39	32.67	1.22							270	0.25	72.59	97			4％	1％
		500	0	0	0	-0.76				5900	STA	475	41.76	82.55	1.02
																				1700	LGC	102	42.39	32.67	1.22								41.76	82.55	1.01			1％
		270	0.25	72.59	97					7600	COL	242	283.1	67.27	3
																						103	42.64	19.86	1.22				1％			243	283.1	25	2.88			4％
1350	HPC	103	42.64	19.86	1.22			-			PUM	CWIN	280.4	15	1.01
																						160	36.15	653.8	59.97							CWINP	280.4	15	2		-0.04
		170	6.5	653.8	59.97							CWOUT	280.4	57.27	1.92			4％
																						501	0	0	0	-29				7820	PUM	246	283.1	67.26	2.77
4100	CBC	160	36.15	653.8	59.97							242	283.1	67.27	3		-0.01
																						320	2.24	25	83.96					6100	MIX	241	263.9	69.96	2.77
		230	16.04	344.4	160							245	19.16	30.02	3
																						405	54.42	1300	58.17			3％	1％			246	283.1	67.26	2.77
5100	EXP	405	54.42	1300	58.17					7810	PUM	244	19.16	30	0.6
																						170	6.5	653.8	59.97							245	19.16	30.02	3		-0.01

Table 14 logistics numerical value: VAST-water circulation (VAST-W) (60)
																				For example, to β=60, TIT=1300 ℃ (～Opt.IRR). The numerical value that runic represents is assumed value
Unit	Title	Logistics	Mass flow kg/s	Temperature EC	The pressure bar	PwrMe   MW	PwrEl   MW	ΔP	ΔQ	Unit	Title	Logistics	Mass flow kg/s	Temperature EC	The pressure bar	PwrMe  MW	PwrEl   MW	ΔP	ΔQ
																						420	60.92	374.2	0.62					6300	SPL	240	283.1	69.96	2.77
		580	0	0	0	84						295	19.16	69.96	2.77
																				6500	ECO	420	60.92	374.2	0.62							241	263.9	69.96	2.77
		430	60.92	120.1	0.61			2％		2300	TRE	295	19.16	69.96	2.77
																						249	16.04	71.58	165							201	16.28	69.97	2.65			4％
		230	16.04	344.4	160			4％	1％	2100	DIS	200	0	15	3
																				7400	FGC	430	60.92	120.1	0.61					8500	DWD	290	2.88	69.96	2.77
		460	41.76	30	0.6			2％		2200	PUM	201	16.28	69.97	2.65
																						243	283.1	25.01	2.88							220	16.28	70.93	100		-0.21
		240	283.1	69.96	2.77			4％		6320	SPL	220	16.28	70.93	100
																						244	19.16	30	0.6				1％			248	16.04	70.93	100
5300	RCP	460	41.76	30	0.6							247	0.25	70.93	100
																						421	41.76	82.59	1.03					7800	PUM	248	16.04	70.93	100
		531	0	0	0	-2.3						249	16.04	71.58	165		-0.14
																				5200	GEN	530				52.2	50.4			Clean electricity output							50

Entrance compression pressure to combination circulates than the VAST-WS that is about 30, and this turbine expansion ratio (β turbine) preferably elects about 76.1 as. To VAST steam circulation (VAST-WS), the pressure ratio of described combination more preferably is adjusted to about 25, so that being increased to, economic performance approaches optimum (table 15, table 16 and table 17 have shown the configuration of the VAST-WS of compression ratio as 25, and collocation method is presented among table 18 and Figure 52). The recompression machine pressure ratio of this VAST-WS circulation preferably is chosen as about 1.81 to obtain about 46.1 the clean turbine expansion ratio of combination (β turbine).

Table 15 device parameter: VAST-water ﹠ steam (VAST-WS)
										For example, 50MW, TIT=1300EC, β=25 (～Opt IRR)
Sequence number	Sign	Designated value			Calculated value
												Polytropic efficiency	T. press from both sides a little	Other	Constant enthalpy efficient		Validity	Surface area	The Q that shifts
			EC					m2	kW
										1310	LPC	0.924			0.9097
1700	LGC			Saturation degree=100%
										1350	HPC	0.924			0.9016
4100	CBC			Excess air=1.05
										5100	EXP	0.8607		Mechanical efficiency=0.98 blade cooling agent/total flow=0.1099	0.9029
6700	SH			T presss from both sides point=15K
										6600	EVA			T presss from both sides point=5K
6500	ECO			Be to the maximum and be lower than boiling point 3EC			0.9321	3,882	9,755
										7400	FGC		5	Saturation degree=100%			0.9332	3,687	53,324
5300	RCP	0.924				0.9177
										5200	GEN			Electrical efficiency=0.985
7100	HX *						0.5003	69	70
										7600	COL		10				0.8	3282	49726
	All pumps		Hydraulic efficiency=0.83; Mechanical efficiency=0.9
										*This adds ordinary circumstance, can remove for this configuration.

Table 16 logistics forms: VAST-water ﹠ steam circulation (VAST-WS)
									For example, 50MW, TIT=1300C, β=25 (～Opt IRR). The numerical value that italic represents is assumed value
Occur for the first time		CH4	H2O(L)	H2O(V)	N2	CO2	O2	Logistics
									Input air	Molar fraction			0.01	0.782	0	0.207	100，101，   102
Mass fraction			0.006	0.762	0.001	0.231
								Behind the intercooler		Molar fraction			0.068	0.737	0	0.195	103，160，   170
Mass fraction			0.043	0.734	0.001	0.222
									Fuel	Molar fraction	0.93			0.07			320
Mass fraction	0.884			0.116
								Behind the burner		Molar fraction			0.508	0.433	0.054	0.005	405
Mass fraction			0.384	0.509	0.1	0.007
									Behind the decompressor				Non-availability				420，430，   431，432
Behind the surface condenser	Molar fraction			0.074	0.8	0.085	0.041	460，421，   475
									Mass fraction			0.046	0.778	0.13	0.045
	Dew-point temperature=40.370 ℃
									The all gas logistics is pure liquid H2O.

Table 17 logistics numerical value: VAST-water ﹠ steam circulation (VAST-WS) (25)
																				For example, 50MW, TIT=1300C, β=25 (～Opt IRR). The numerical value that runic represents is assumed value
Unit	Title	Logistics	Mass flow Kg/s	Temperature EC	The pressure bar	PwrMe   MW	PwrEl   MW	ΔP	ΔQ	Unit	Title	Logistics	Mass flow kg/s	Temperature EC	The pressure bar	PwrMe   MW	PwrEl   MW	ΔP	ΔQ
																				The input logistics
1100	OXS	100	42.47	15	1.01
																				2100	DIS	200	0	15	3
3100	FUS	320	2.25	25	35.75
																				Equipment and logistics
1200	TRE	100	42.47	15	1.01					5300	RCP	460	42	30	0.57
																						101	42.47	15	1			1％				421	42	88.3	1.03
1310	LPC	101	42.47	15	1							531	0	0	0	-3
																						102	42.47	151	3.54					5200	GEN	530				52	50
		500	0	0	0	-6				7100	HX	421	42	88.3	1.03
																				1700	LGC	102	42.47	151	3.54							475	42	86.7	1.02			2％
		270	1.65	78.3	9.7							247	1.65	68.3	10
																						103	44.13	64.1	3.54				1％			270	1.65	78.3	9.7			4％	1％
1350	HPC	103	44.13	64.1	3.54					5900	STA	475	42	86.7	1.02
																						160	37.41	336	25.53								42	86.7	1.01			1％
		170	6.72	336	25.53					7600	COL	242	292	65.7	3
																						501	0	0	0	-13						243	292	25	2.88			4％
4100	CBC	160	37.41	336	25.53						PUM	CWIN	290	15	1.01
																						320	2.25	25	35.75							CWINP	290	15	2		0.039
		230	6.18	219	25.66							CWOUT	290	55.7	1.92			4％
																						231	8.63	462	24.89
		405	54.47	1300	24.77			3％	1％

Table 17 logistics numerical value: VAST-water ﹠ steam circulation (VAST-WS) (25)
																				For example, 50MW, TIT=1300C, β=25 (～Opt IRR). The numerical value that runic represents is assumed value
Unit	Title	Logistics	Mass flow Kg/s	Temperature EC	The pressure bar	PwrMe   MW	PwrEl  MW	ΔP	ΔQ	Unit	Title	Logistics	Mass flow kg/s	Temperature EC	The pressure bar	PwrMe  MW	PwrEl   MW	ΔP	ΔQ
																				5100	EXP	405	54.47	1300	24.77
		170	6.72	336	25.53
																						420	61.19	477	0.59					7820	PUM	246	292	65.7	2.77
		580	0	0	0	73						242	292	65.7	3		0.007
																				6700	SH	420	61.19	477	0.59					6100	MIX	241	273	68.2	2.77
		430	61.19	420	0.59			2％				245	19.2	30	3
																						252	8.63	225	25.66							246	292	65.7	2.77
		231	8.63	462	24.89			2％	1％	7810	PUM	244	19.2	30	0.57
																				6600	EVA	430	61.19	420	0.59							245	19.2	30	3		0.006
		431	61.19	230	0.58			2％		6300	SPL	240	292	68.2	2.77
																						251	8.63	219	25.66							295	19.2	68.2	2.77
		252	8.63	225	25.66				1％			241	273	68.2	2.77
																				6350	SPL	250	14.81	219	25.66					2300	TRE	295	19.2	68.2	2.77
		230	6.18	219	25.66							201	16.5	68.2	2.65			4％
																						251	8.63	219	25.66					2100	DIS	200	0	15	3
6500	ECO	431	61.19	230	0.58					8500	DWD	290	2.77	68.2	2.77
																						432	61.19	112	0.58			2％		2200	PUM	201	16.5	68.2	2.65
		249	14.81	68.5	26.46							220	16.5	68.3	10		0.016
																						250	14.81	219	25.66			4％	1％	6320	SPL	220	16.5	68.3	10
7400	FGC	432	61.19	112	0.58							248	14.8	68.3	10
																						460	41.95	30	0.57			2％				247	1.65	68.3	10
		243	292.3	25	2.88					7800	PUM	248	14.8	68.3	10
																						240	292.3	68.2	2.77			4％				249	14.8	68.5	26.46		0.033
		244	19.24	30	0.57				1％	Clean electricity output							50.0

Table 18 is used for the computational methods of VAST-W ﹠ S (β=25)
1	Set fixed variable: (numerical value of demonstration is the numerical value for this actual configuration)
													T(F100)＝15℃				P (F100)=1.01 bar		X (F100)=[referring to forming explanation]
		T(F200)＝15℃				P (F200)=3 bar
													T(F320)＝25℃				P (F320)=35.75 bar		X (F320)=[referring to forming explanation]
													Overall pressure ratio (β)=25
		Pressure drop (Δ P) and heat loss (Δ Q) to all devices that shows in the logistics numerical tabular
		The cold Δ T=3 of mistake among the logistics F276 ℃
		T (cooling water)=15 ℃
													Temperature among 7600 (COL) folder point=10 ℃
		Temperature among 6700 (SH) folder point=5 ℃
													Temperature among 6600 (EVA) folder point=5 ℃
		Temperature among 7400 (FGC) folder point=5 ℃
		The polytropic efficiency of 1310 (LPC)=0.9240
													The polytropic efficiency of 1350 (HPC)=0.9240
		The polytropic efficiency of 5100 (EXP)=0.8607
													The polytropic efficiency of 5300 (RCP)=0.9240
													P(F276)＝P(F160)
		T (F276) is excessively cold=and 3 ℃
		Logistics F103 (leaving the gaseous state logistics of 1700 LGC) is saturated for H2O
													Logistics F460 (leaving the gaseous state logistics of 7400 FGC) is saturated for H2O
		Actual O2 is to stoichiometric ratio=1.05
													T(F405)＝1300℃
													Total flow in blade cooling agent/decompressor=0.1067
		The mechanical efficiency of decompressor 5100 (EXP)=0.98
													The electrical efficiency of generator 5200 (GEN)=0.985
		The hydraulic efficiency of all pumps=0.83
													The mechanical efficiency of all pumps=0.9
													T(F475)＝86.72
													The compression ratio of getting two compressors is 25
											2	Primary Calculation
		Calculate 1200 (TRE) to obtain X (F101), P (F101) and T (F101)
												Calculate T (F276) according to crossing cold numerical value
		Temperature folder point among T (F244)=T (cooling water)+7600 (COL)

Table 18 is used for the computational methods of VAST-W ﹠ S (β=25)
							3	Initial designs variable: (show value=selected value)
		P (F102)=3.54 bar				P (F420)=0.59 bar
								4	β, Δ P ' s and the design variable pressure that calculates all logistics from supposition
	5	Suppose base value F101=1kg/s, and calculate 1310 (LPC) to obtain W500, F102 and T (F102) according to X (F101).
								6	Conjecture T (F270) (final value after the iteration :=219.30 ℃)
		(note: because the value of F270 is less, described calculating is not very responsive to this value)
									7	Suppose that logistics F103 is saturated, and calculate 1700 (LGC) to obtain F270, F103, X (F103) and T (F103).
		8	Calculate 1350 (HPC) to obtain F160, T (F160), W501 and T (F170)
									9	Conjecture F270 (final value after the iteration=6.18kg/s)
			10	Conjecture T (F275) (final value after the iteration=461.70 ℃)
											11	Suppose base value F320=1kg/s fuel. Based on X (F320), the excessive O2 ratio of supposing and T (F405) calculate 4100 (CBC) to obtain actual F160, F275, F405, X (F405)
				12	According to the ratio of blade cooling agent to the total flow by decompressor, calculate F170
											13	According to the polytropic efficiency of appointment, calculate 5100 (EXP) to obtain F420 and T (F420)
			14	Check T (F420)-T (F275)=whether the temperature folder point of 6700SH permission is set up. If be false, adjust T (F275) and begin to compute repeatedly from step 10. If set up, continue.
										15	Get F251=F275, calculate 6350SPL to obtain T (F251), F250, T (F250)
			16	According to P (F252), and the hypothesis saturated vapor, T (F252) calculated
										17	Calculate 6700SH to obtain F430, T (F430)
			18	Calculate 6600EVA to obtain F431, T (F431)
									19	Check T (F431)-T (F252)=whether the temperature folder point of 6700SH permission is set up. If be false, adjust F270 and begin to compute repeatedly from step 9. If set up, continue.
		20	According to the summation of F160 and F170, adjust F103, F102, F270, F101. F100=F101
									21	Conjecture T (F248) (68.29 ℃ of the final values after the iteration)
			22	Calculate 7800 (PUM) to obtain F249, T (F249)
										23	Calculate 6500 (ECO) to obtain F430, T (F430)
			24	Temperature folder point according to saturated vapor F460 and 7400FGC calculates 7400 to obtain F460, T (F460), X (F460), F244, F240, T (F240), F246, T (F246)
										25	Get F295=F246 and calculate 6300SPL to obtain T (F295), F241, T (F241)
			26	Get F201=F249+F270
										27	Calculate 2300 (TRE) to obtain F200 or (F290 and T290)
			28	Calculate 2200 (PUM) to obtain F220, T220
										29	Calculate 6320 (SPL) to obtain T (F248), F255, T (F255)
		30	Does T (F248) meet the T (F248) of hypothesis in the step 21? if not, adjust T (F248) and begin to compute repeatedly from step 21. If so, continue.
									31	According to its polytropic efficiency, calculate 5300 (RCP) to obtain F421 and T (F421).
		32	According to the T (F475) of appointment or to the explanation of the number of degrees that are higher than saturation degree, calculate 7100HX to obtain F270 and T (F270)
								33	Does T (F270) meet the T (F270) of supposition in the step 6? if not, adjust T (F270) and begin to compute repeatedly from step 6. If so, continue.

Table 18 is used for the computational methods of VAST-W ﹠ S (β=25)
				34	Calculate 6100 (MIX) to obtain F242, T (F242)
	35	Calculate 7820 (PUM) to obtain F243, T (F243)
				36	Calculate 7600 (COL)
	37	Calculate all heat exchanger areas
				38	Calculate all capital costs and Master Cost and generating quantity

With reference to Figure 39, by two or more compressors, can change described high pressure to low pressure compressor, to improve system effectiveness.

Excessive water injects loss vs drag losses (Drag Losses)

Drag losses by one or more assemblies and/or parasitic pumping loss have reduced effective oxidant compression ratio, and and then have reduced the clean turbine expansion ratio that can be used for the recovery mechanical energy. For example, one or more inlet diffusers, entrance oxidant fluid filter, inlet water carry in the sprayer, compressor in the middle of water spray device, the compressor that surperficial intercooler, diffuser, burner assembly comprise diffuser, fluid conveying device and equilibrium area (" changeover portion "), superheater, evaporimeter, economizer, preheater, condenser, cooler and diffuser in the middle of water spray device, the compressor secretly. In order to reduce pressure drop, the user preferably disposes water spray formula oxidant inlet filter, for example ' instructs in 191 patent applications. Also preferably dispose the direct contact type condenser and reduce pressure drop and improve hot property, for example ' instruct in 191 patent applications.

The multiaxis turbine machine

In certain embodiments, the user is preferably at axle configuration first compression turbine and first compressor. Preferably place power turbine and generator at the second axle. The user preferably disposes the recompression machine with described compression turbine and compressor on the first axle. Preferred described combination and motor fit together, but the speed of this motor punching out compressor-recompression machine combination. In other configuration, described recompression machine and motor are configurable on axle independently.

This combination provides the flexibility when changing described compressor-turbine rotating speed with the relevant flow velocity that contains oxidant fluid and combustion process. Because it needn't drive compressor, therefore described power turbine preferably disposes to provide required torque and speed to application. For example, it can be configured to and carry high torque (HT) in low-speed applications. Similarly, described turbine and generator can be on axles independently, with the proportional fixed speed operation of described screen speed.

The rotating speed of at least one turbine can be heightened or reduce, thereby moves this turbine under more efficient parameter. For example can adjust according to required output shaft speed the speed of described power turbine. Similarly, can change the speed of described recompression machine to control clean turbine expansion ratio.

In some configuration, the user can dispose adjustable-speed driver between described power turbine and output driving shaft. This can adapt to most speed change, keeps simultaneously described turbine near its optimum efficiency to power demand.

Preferably the power with described compression turbine is adjusted to the required power of described compressor. When the O2 concentration of emission was 15% under the unit compressed air require, this burnt the compression turbine than conventional fuel-sean and reduces about 65% to about 72%. When the user adds the recompression machine, preferably described compression turbine is adjusted to the general power that two compressors on described the first axle extract.

In certain embodiments, the user preferably disposes second (low pressure) compression turbine or electro-motor at the 3rd axle, disposes simultaneously the entrance low pressure compressor. In this class configuration, the user preferably at the 3rd axle configuration recompression machine, places on the first axle high pressure compressor with the high pressure compressed turbine simultaneously again. Described high pressure compressed turbine is configured to the required power of relevant compressor with low pressure compression turbine or electro-motor. The user preferably directly uses described power turbine or uses with generator on the second axle independently.

Some embodiment is connected mechanical device with described turbine, medium drive can be used or do not used to described connection. Except compressor, mechanical device can be made of at least one container propeller, circulation recompression machine and circulating pump.

The clean specific power of turbine

In certain embodiments, the user preferably promotes net power or " specific power " of the unit mass flow of turbo-expander. That is, the clean turbine output kW of unit turbine mass flow (kg/s)=(kJ/s)/(kg/s)=(kJ/kg). By improving the producible power of same turbine, can reduce the capital investment that the VAST circulation produces power demand. Because annual use hourage reduces, therefore this investment becomes power cost ($/kW, the major part of or energy cost ￠/kWh or $/MWh) day by day.

In some configuration, the user preferably disposes described VAST circulation, so that following characteristic and benefit to be provided:

Improve the turbine specific power of every workshop section

Higher specific heat capacity

Higher specific enthalpy

Quality to given power ratio is lower

To higher to the power of fixed temperature, mass flow, pressure

Higher peakedness ratio power

Higher turbine expansion ratio

Clean turbine expansion ratio

In certain embodiments, the user preferably improves the expansion ratio of described turbine, and wherein high-energy fluid expands by this turbine. That is, described expansion ratio is that the high pressure of turbine inlet is to the ratio of the low pressure after the turbine outlet.

In some configuration, the vaporized diluent that the user pumps in order to liquid state substitutes the major part in the hot diluent of gaseous state of excessive oxidant and compression. Preferably according to the size of adjustment compressor of the present invention and turbine. (for example, by pumping into water alternative about 65% or more compressed air). This so that the clean turbine output of the unit turbine mass flow of the high-energy fluid by described turbine or clean specific power significantly rise (high-energy fluid that the high-energy fluid that the turbine inlet of the every kg/s flow of kW detects or kJ/kg turbine inlet detect) (referring to, for example Figure 41 and Figure 48). Therefore, this relative prior art has significantly improved the torque from power turbine, particularly in low speed.

For example, to the air of 1300 ℃ of the sample industry 50MW turbine of deriving, by the VAST steam circulation (VAST-WS) with steam and the recovery of hydro-thermal amount, air pressure about 30 is than (near the economic optimum value) under the β, and the clean turbine output of the clean turbine output unit turbine mass flow of unit turbine mass flow is about 843kJ/kg (kW/kg/s). The scope of this power for from air pressure than β be about 10 o'clock about 791kJ/kg to air pressure be about 40 o'clock about 852kJ/kg than β.

Similarly, to the air of 1300 ℃ of the sample industry 50MW turbine of deriving, by the VAST-W (VAST water circulation) that only has the hydro-thermal amount to reclaim, air pressure about 30 is than (near the industrial economy optimal value) under the β, and the clean turbine output of the clean turbine output unit turbine mass flow of described unit turbine mass flow is about 847kJ/kg (kW/kg/s). The scope of this power for from air pressure than β be about 10 o'clock about 764kJ/kg to air pressure be the peak value of about 40 o'clock about 851kJ/kg than β. Be about at 58 o'clock at pressure ratio β, this clean turbine specific power falls after rise to about 848kJ/kg.

In certain embodiments, the preferred water of user or steam substitute the cooling of turbine blade air, or do not use the turbine blade cooling. Reclaim with steam and hydro-thermal amount but do not have air cooled VAST steam circulation (VAST-WS), the pressure ratio β to about 50 to about 10 can realize respectively higher hot diluent/oxidizer flow rate (water/air) ratio of about 41% to about 44%. Therefore, this configuration obtains much higher clean turbine specific power.

Near about 30 air pressure of industrial economy optimal value than under the β, this can not realize the clean turbine specific power of about 980kJ/kg (kW/kg/s) with the VAST-WS of blade cooling. The scope of this clean turbine specific power is to the about 50 o'clock about 993kJ/kg of pressure ratio β from the about 10 o'clock about 912kJ/kg of pressure ratio β.

By compared with the prior art, under conditions of similarity, the clean specific power of turbine of the most similar HAWIT circulation is about 612kJ/kg (kW/kg/s). (that is, the general power of turbine deducts all the pumping merits in compressor and the pump, again divided by the fluid mass flow that leaves described turbine. That is, the clean specific power of the turbine of described VAST-WS exceeds about 38%. Similarly, the clean specific power of turbine of single pressure STIG circulation is 533kJ/kg. Like this so that described VAST-WS circulates high about 58% than STIG aspect the clean specific power of described turbine. These parameters provide huge thermoeconomics benefit.

Similarly, in the turbine example that this 50MW industrial air is derived, described is not 980kJ/kg with the clean turbine specific power of blade cooling and air cooled VAST-WS, and it is high by 60% to circulate than HAWIT approximately, and it is high by 84% to circulate than STIG.

It should be noted that also described VAST circulation adopts the ratio of the hot diluent of very high adding/contain oxidant fluid flow (in the suction port of compressor) (for example total water that adds/always compress air mass flow). The example that for example air-cooled turbine is calculated when 1300 ℃ of the turbine inlet temperatures, this ratio is 29%-40%. Comparatively speaking, described four kinds of prior art circulation STIG, HAT, RWI and HAWIT in the water/AIR Proportional of conventional air pressure during than 20-40 usually in the 12-23% scope. (the new design of supposition complete alternation is so that can add other diluent of this level). Therefore, in the time of about 1300 ℃, VAST circulation preferably provide be higher than 26% always add entry/always compress air mass flow. At lower turbine inlet temperature (TIT), these water/AIR Proportional further improve.

The turbine requirement

High-temperature fuel gas wheel thermomechanical components needs in the high-energy fluid ion concentration such as sodium and vanadium lower, damages to avoid assembly. Its preferred fine grain level is lower, and to avoid turbine fin and blade fouling, this fouling meeting lowers efficiency. These harmful constituents contain oxidant fluid, fuel and hot diluent from input. (for example, compressed air, diesel fuel and water).

Component cooling ﹠ recycles the heat of cooling

The user preferably provides hot diluent cooling (referring to Figure 18 and Figure 22) to one or more heat generating components. For example, can cool off one or more in generator, motor, thermo-mechanical drive, pump, bearing, electromagnetic transducer (for example transformer or frequency conversion converter) or the electromagnetic controller. With reference to Figure 18, these can be used as low temperature and describe and collect. Then preferably the fluid after the described heating is sent back to described VAST thermodynamics circulation, with cooling combustion process and high-energy fluid. This class coolant flow has reclaimed the heat that usually runs off by assembly, thus the fuel amount that has needed when having reduced the temperature that will leave the high-energy fluid of burner and being increased to required burner outlet temperature (or turbine inlet temperature).

Described turbine-generator drive system is the important source of heat loss. In certain embodiments, the heat that the described drive system of the preferred recovery section of user produces, and with hot diluent it is recycled.

Speed change electronic power converter/controller can be realized about 95% to about 96% efficient. For example, in small-sized turbine dynamical system. Therefore, have an appointment in the general power that generator produces and 5% change into heat to 4%. Converting system powered by conventional energy provides air to cool off to keep the temperature of described electronic power converter usually. The air-supply power of described fan is huge parasitic loss, and lowers efficiency.

As an alternative, by the VAST circulation, the user preferably provides liquid heat exchanger to come the cooling power electronic device in some configuration. The flow that the user preferably disposes described heat exchanger and/or controls described hot diluent to keep the junction temperature of power converter to be lower than required or desired level (or be reduced to desired level with fault rate) according to reliability requirement. The user preferably provides pump more than needed, thereby provides the cooling agent fluid with required probability.

By this measure, reclaim heat in user's driven force electronic device, and hot diluent is heated to the approaching temperature of leaving described drive electronic device heat exchanger that allows from the fluid temperature (F.T.) of leaving described condenser. For example, choose temperature about 25 ℃ to about 30 ℃ hot diluent, and be heated to and be up to about 95 ℃ to about 98 ℃. Therefore, the user has reclaimed about 3.5-4.5% or more power, otherwise these heats will lose with the heat form from the freq-variable electronic power converter.

Hot diluent after the user preferably will heat is conveyed in the hot diluent flow of the described high-energy fluid of one or more strands of common coolings. This has reduced to act as a fuel to add and will contain the heat that oxidant fluid and hot diluent temperature are promoted to required burner outlet temperature (or turbine inlet temperature). By this heat of preferred recovery, the thermal efficiency obviously rises.

For example, about one percentage point or more. By these measures, estimate in the small-sized turbine dynamical system of 100kW, to reclaim the heat of 3.5-4.5kW. Reduced simultaneously required parasitic fan power. Therefore, in this class system, expectation can be promoted to about 37% from about 36% with the efficient of the small-sized turbine dynamical system of this 100kW VAST.

In the configuration of this class, preferably use the material of low-solubility high conductance or coating as the lining of described heat exchanger, decompose the degree that (dissolution) enters hot diluent to reduce described heat exchanger. For example, zinc-plated or stainless steel coating reduces corrosion or the decomposition of copper heat exchanger. This has reduced copper in the described hot diluent system or the concentration of other alloy (these alloys can flow in the turbine with high-energy fluid).

Gear train produces 0.5-2% or higher loss usually. In certain embodiments, the user preferably cools off described gear train and reclaims these heats with the fluid cooling agent. Preferably described hot diluent directly is used as the fluid cooling agent. In other configuration, use the intermediary cooling agent that is fit to, and subsequently heat is recovered in the hot diluent.

In some configuration, the user preferably provides lubricated with described hot diluent and the heat cooling simultaneously. For example, the high purity deionized water that is used as hot diluent contains few particulate, and can be used as lubricant and cooling agent. In this class configuration, the user preferably uses corrosion-resistant material to described gear train.

The varying-speed machinery driver has similar loss and lubricated demand. In some configuration, the user preferably cools off described driver and reclaims described heat with hot diluent. When suitable the time, preferably lubricate simultaneously described driver with this hot diluent, or cool off described lubricant with this hot diluent.

Generator

Because electric current flows in conductor, so generator has obvious ohmic loss. Its same generation windage (windage) loss. Generator is normally air cooled, and heat loss. Generator loss is 5% to small-sized alternating current generator approximately, is 1.5-2% to high-speed small-size permanent magnet generator, and high-rating generator is down to 0.5-1.25%. In improved embodiment, the speed (being temperature) of removing heat from described generator can change to change generator (AC or DC) power output.

In some configuration, the user preferably hot diluent is carried by and/or the surrounding rotor stator so that it is cooled off, and reclaim most engine loss. The preferred use by the diluent of the application of more heat-sensings such as the heating of drive electronic device. Preferably use high-temperature insulating coating at coil and/or permanent magnet, at high temperature operating described generator, and the described heat energy of recovery and reuse more effectively.

When cooling off generator amature with gas, the user preferably provides heat exchanger to come to reclaim heat the gas after these are heated. For example, cooling is used for the hydrogen of cooling large-scale generator rotor, with the while cooling conductor and reduce windage.

Recompression machine (RCP)

With reference to Figure 25, the user preferably makes described high-energy fluid be expanded to be lower than atmospheric pressure, to be condensed to the condensable diluent fluid that contains of small part, subsequently atmospheric pressure is got back in incondensible material recompression. 5300 pairs of useless (spent) fluids of this recompression machine operate, this fluid mainly is moistening combustion product, namely mainly by residual uncooled water vapour saturated nitrogen and carbon dioxide, and contain some excessive oxygen and inert gas (such as argon).

The user is preferably expanded to high-energy fluid as mentioned above and is recompressed, contain the diluent fluid by heating and evaporation again subsequently and come from described expansion fluid, to reclaim heat, and this is contained between the diluent fluid injection expansion workshop section (referring to Figure 26 and Figure 31). This has additionally reclaimed the part heat, and extra gas is injected the decompressor formation, to produce extra mechanical power.

When the compression of other needs, the user preferably recompresses combustion product but not described reactant gas, to reduce compressed gaseous mass flow rate. In combustion process, described oxidant and fuel reaction form carbon dioxide and water. Water is preferably also as hot diluent. The water that preferably will form with add condensation and removing in condenser. Compare with reactant gas, this significantly reduced uncondensable material volume in the described combustion product (except common uncondensable diluent gas for example nitrogen, excessive oxygen and comprise the inert gas of argon gas).

For example, one mole of methane and two moles of oxygen reactions obtain one mole of carbon dioxide and two moles of water. Make so incondensible gas volume reduce by 67%, become one mole from three moles. Similarly, when burning diesel oil machine fuel, be reduced to 12 moles of carbon dioxide and 13 moles of water from about 18.5 moles of oxygen. This is so that these uncondensable reactions and product gas have reduced about 35%.

Cool off described expansion fluid by preferred with the direct contact type condenser, the user preferably obtains very the temperature near described cooling agent fluid. For example, near external environment. This is usually less than the mean temperature that contains oxidant fluid of compression in high pressure compressor (HPC) 1350. Therefore, described fluid density is higher, and this has reduced the cost of described compressor with respect to the higher fluid of compression temperature.

By this before turbine 5100 compressor and recompression machine 5300 conglomerations (hybrid combination) behind the turbine 5100, preferably reduce simultaneously the cost of described compressor and running.

In the embodiment of the discharging fluid being cooled off with condensation, the user preferably adds recompression machine 5300 described expansion fluid is discharged back atmosphere. Described cooling and condensation have reduced the volume of the gas of described expansion. Therefore, by recompression machine 5300, the pressure in described turbine downstream is brought down below atmospheric pressure. The user preferably adopts this configuration to improve net heat mechanics cycle efficieny and cost (referring to Figure 37, Figure 50, table 1, table 19 and table 20).

The relative cost 50MW TIT=1300EC configuration of the selected VAST circulation of table 19**
							Assembly	VAST-water@β=30		VAST-water@β=60～OptIRR		VAST-water ﹠ steam@β=25～Opt IRR
	Cost USD	The % of TCI	Cost USD	The % of TCI	Cost USD	The % of TCI
							Compressor Lpc	750,792	3.80％	166,151	0.99％	1,121,085	6.07％
Compressor Hpc	2,509,092	12.69％	2,267,265	13.47％	1,916,905	10.38％
							The Vast burner	41,911	0.21％	40,911	0.24％	42,336	0.23％
Decompressor	2,289,130	11.58％	2,355,036	13.99％	1,940,043	10.50％
							Superheater					225,706	1.22％
Evaporimeter					367,342	1.99％
							Economizer	425,243	2.15％	409,328	2.43％	457,117	2.47％
The fuel gas condenser	231,549	1.17％	307,774	1.83％	323,118	1.75％
							The recompression machine	1,203,887	6.09％	458,852	2.73％	508,453	2.75％
Water preheater	49,353	0.25％	3,451	0.02％	28,072	0.15％
							Cooler	269,186	1.36％	301,633	1.79％	301,318	1.63％
Pump recirculation (to cooler)	9,877	0.05％	8,041	0.05％	8,507	0.05％
							Pump recirculation (Condtocoo)	5,619	0.03％	6,204	0.04％	6,280	0.03％
Pump boost (to Hrecov)	70,605	0.36％	78,786	0.47％	12,672	0.07％
							Pump charging (to the vast blender)	49,761	0.25％	58,385	0.35％	20,841	0.11％
The pump cooling water	27,000	0.14％	21,984	0.13％	22,489	0.12％
							Generator	1,836,380	9.29％	1,837,818	10.92％	1,827,379	9.89％
The equipment cost of buying	9,769,385	49.42％	8,321,619	49.42％	9,129,663	49.42％
							Indirect cost	9,996,928	50.58％	8,515,440	50.58％	9,342,307	50.58％
Total capital investment TCI	19,766,31   3	100.0％	16,837,059	100.0％	18,471,970	100.0％
							The salvage value of supposing	0		0		0
Capital investment $/MW	15.0		12.8		14.1
							Variable cost $/MWh	30.6		30.5		30.5
Totle drilling cost US $/MWh	45.6		43.3		44.6
							Cost equation according to the Traverso 2003 in the table 3; Average industrial its cost to US 2000

Table 20VAST recycle compressor, recompression machine beta ratio ﹠ turbine expansion ratio
																	VAST-W				VAST-WS				VAST-WSR
β		RPC   LPC	RPC   HPC	RPC   (LPC*HPC)		EXP	RPC   LPC	RPC   HPC		RPC   (LPC*HPC)	EXP	RPC   LPC	RPC   HPC	RPC  (LPC*HPC)	EXP
																10		3.903	0.873	0.585		58.09	1.463	0.942		0.372	36.96	2.371	1.104	0.542	42.946
20		2.134	0.633	0.260		103.44	1.348	0.326		0.148	59.01	1.184	0.576	0.185	73.506
																30		1.211	0.351	0.119		105.89	0.806	0.269		0.085	76.13	1.067	0.3	0.104	92.563
40		0.863	0.224	0.070		107.91	0.786	0.169		0.058	91.53	0.668	0.245	0.064	101.936
																50		0.964	0.108	0.046		112.56

Liquid state-gaseous fluid contact device

Some embodiment adopts the gaseous fuel that is rich in carbon dioxide, as the confession carbon product of food production, energy crop production, aquatic products industry or mariculture. Formed " VAST gas^TM" be generally 300% (referring to, table 3 for example) that O2 in the discharging gas accounts for 15% conventional poor aflame amount of carbon dioxide.

In these embodiments, the NOx concentration of formation is very low, and using for this class provides very suitable carbon supply. This has significantly reduced the accelerate the ripening effect of plant, fruit or other gardening product of NOx. In other configuration, when needs initiatively improve or during hasting of maturity, user's temperature in the combustion chamber 4100 that preferably raises is to improve NOx output.

High humility in the discharging gas is used ideal to gardening.

In other embodiments, user's sub-argument from exit gas goes out carbon dioxide, and provides the gas that is rich in carbon dioxide to medicine production, biosynthetic process or the application of other high-carbon.

In certain embodiments, preferably described carbon dioxide content is the abundant or gas that is rich in carbon dioxide as overflow (flooding) fluid in the petroleum recovery process. In other embodiments, the user seals carbon dioxide up for safekeeping (sequester) in deep water, particularly in the area or geologic structure of oil exhaustion, to reduce the greenhouse effects that worsened. Described embodiment provides more efficient and the effective method of cost reclaims and utilize or seal up for safekeeping described carbon dioxide.

Diffuser/chimney

In certain embodiments, the user preferably controls through in the coolant flow of described expansion fluid condenser 7500 and these two parameters of recompression motor speed one or two and regulates the recompression ratio. These have controlled the pressure of expansion fluid F420 and the gas temperature of expansion fluid. The parameter that relates to water/fuel ratio, air/fuel ratio and propellant composition by controlling these, the user preferably adjusts the dew point of the waste fluid (or " flue gas ") of discharging. So, can be adjusted in the hot diluent mark of condensation in the condenser 7500. (for example, the mark of recycle-water or speed). Preferred composition and temperature of regulating waste fluid F475 makes its temperature be higher than its dew point or saturation temperature. By this control, can avoid the condensation in diffuser or chimney 5900.

Cool off described turbine discharging gas, the described hot diluent of condensation and recompress described uncondensable waste fluid produces undersaturated flue gas usually. So, can be reduced in the size of the visible column of smoke (plume) that forms at described exhaust apparatus under the common external condition, or with its elimination. In some configuration, can control or reduce the dew point of discharging gas, thereby when the Shi Buhui formation column of smoke that described discharging fluid is discharged into the atmosphere.

This public who is of value to around making feels that this is the dynamical system of clean environment. It also provides a kind of approach to satisfy local regulation, for example in the urban area the visible column of smoke mustn't be arranged. This is so that can be placed in this class VAST circulatory system the municipal administration area of forbidding forming the column of smoke. Compare with the method that prevents the column of smoke with heating described discharging gas in the prior art, it provides more effective and economic method to control the column of smoke again. This recompression VAST circulation has these advantages, and need not come flue gas is heated again with stove and fuel etc.

Control system

Certain embodiments of the present invention preferably include controller, it preferably controls and monitors the overall operation of described system, for example filter pressure drop, pump head, pump speed, compressor and/or blower speed, burner pressure and temperature, expansion crankshaft torque, generator output etc. As requested or need, can use suitable sensor, for example rotating speed, pressure, temperature, flow gauge etc. Described controller can be integrated reponse system effectively.

Preferably described controller is configured to control the conveying of diluent in the VAST thermodynamics circulation of disposing. Such as Figure 28 and shown in Figure 29, according to flowing of required guiding liquid state and gaseous diluent, to reclaim heat or cooling high-energy fluid. Similarly, according to the temperature that be heated with control or heat generating component that flows of required guiding diluent fluid or cooling agent fluid, such as Figure 18 and shown in Figure 22. Described controller is preferably controlled cooling agent or diluent flow to the one or more hot assembly of described combustion system and described expansion system.

According to appointment, the diluent after the heating can be sent to the application of using heat, for example Figure 28 and shown in Figure 29. Such as Fig. 8, Figure 12 and shown in Figure 13, when containing oxidant fluid and compress, preferably cool off the one or more strands of oxidant fluids that contain with diluent. Described controller preferably distributes described logistics in these are used, to satisfy relevant cooling and temperature control criterion.

The user preferably controls described diluent flow, its temperature that satisfies the assembly that will be heated is controlled at is lower than selected design temperature. When the heat-sensing assembly was carried out initiatively cooling off, the user preferably preferentially provided diluent flow to hold it in to be lower than corresponding design temperature. Sensor such as temperature or flow sensor preferably is provided, comes temperature sensor or flow regime. When diluent mass flow is not enough to according to required control temperature, preferably takes measures to control described flow and initial power reduction, or take other measure.

Similarly, some heat is used the diluent that is heated that needs minimum flow. Usually need its temperature to be higher than minimum temperature. Therefore, the user preferably controls described diluent or coolant flow, to guarantee that minimum temperature is in required probability. For example, reclaim heat from high-energy fluid. For this purpose, preferably described turbine inlet temperature is controlled at and belongs to required scope, for example be lower than the design boundary of turbine inlet temperature and be higher than actual temperature, this actual temperature is enough to realize leaving the minimum demand temperature of described heat recovery system. Preferably carry the diluent fluid through described recuperation of heat heat exchanger to flow with flow-controllable, to obtain required degree of heat and the fluid temperature (F.T.) that is sent to required application.

Preferred control fuel flow rate comes by required heat and machinery or the electrical power of described Conversion of Energy system's acquisition. When power level fluctuates, regulate preferably that diluent mass flow is controlled at required temperature with described turbine inlet temperature or in required scope.

When control temperature sensitive assembly, hot fluid temperature and motivation level, the user preferably is sent to the part diluent oxidant delivery system cooling off compressed described oxidant fluid, and improves the efficient of compression process. When the diluent of can vaporizing sprayed in the compressed oxidant fluid, the amount that the user preferably will carry was controlled at and is lower than required design level. Preferably carry out these and arrange to avoid the compressor surging. Equally also can adjust it, and adjust the drop size of liquid diluent and/or temperature so that diluent evaporates in required separation distance, and reduce or avoid compressor to corrode. Preferably carry the multiply logistics between the entrance of described compressor and each the compressor workshop section, with the oxidant strengthening cooling and make compression near saturation state.

Similarly, the user disposes remaining diluent in described heat recovery system, to improve specific power and cycle efficieny in realization these other control target. When in the urgent need to the fluid of heat, the user in addition can with temperature or not the liquid diluent of heating send in the described burner and control turbine inlet temperature, and cool off similarly the burner bushing pipe. For example, warm water or cold water are sent into burner and suitably replenished available steam and/or hot water with temperature and the turbine inlet temperature of control high-energy fluid. This provides the method that described energy conversion system obtains multiple and/or different purposes of controlling flexibly.

Summary

By above-mentioned explanation, be to be understood that to herein disclosed is with one or more methods as herein described to make up the thermodynamics circulation of using liquid diluent. Although described to a certain extent the details of assembly of the present invention, technology and aspect, be to be understood that under the prerequisite that does not break away from spirit and scope disclosed herein, in specific design described herein, structure and method, can carry out various modifications.

When providing concrete size, its just with exemplary purpose provide but not regularity. Certainly, will be understood by those skilled in the art that one or more benefits or advantage in order to realize that this paper instructs or points out, as requested or need fluid component, pressure, temperature, heat flow and the power level that also can effectively adopt other to be fit to.

Although, to some embodiments, some compressor, heat exchanger, turbine, pump, treatment system, pipeline, valve, blender and other assembly have been shown in some configurations, but can effectively use the combination of these configurations, comprise that the type and method, temperature control, the power that change described compressor size, compressor workshop section quantity, compression ratio, turbine size, turbine expansion ratio, workshop section's number, heat exchanger size, surface heat exchanger or direct heat exchanger, logistics control are controlled, enthalpy control, also can use other to be used for size and the parameter of thermodynamics circulation.

Although in certain embodiments, use turbine as decompressor, also can use the decompressor of other type, comprise reciprocating expansion engine.

When using these terms of fuel, diluent, water, air, oxygen and oxidant, described method can generally be applicable to other combination or other other combination reactive or non-reacted fluid of these fluids. When relating to fluid quantity, these methods can generally be applicable to comprise quantity and the continuous fluid flow of gradation conveying. When being described to assembly method, can effectively adopt various alternative assembly methods to be configured, this paper instructs or benefit or the advantage of one or more embodiments of prompting to obtain.

When relating to laterally, axially, radially, when circumference or other direction, be to be understood that the conventional coordinate system of any use curvilinear coordinate all can use, comprise Descartes, cylinder, spherical coordinate system or other specialized system, such as loop system. Similarly, when relating to laterally one or more or axially distributing or during section, be to be understood that as required or indicate described configuration and method can be applied to similarly space control in one or more direction of a curve. Similarly, described contactor, formation, device or pipeline direction can be reset in a usual manner, to obtain other useful combination of described method and feature.

Although described to a certain extent the details of assembly of the present invention, technology and aspect, be to be understood that under the prerequisite that does not break away from spirit and scope disclosed herein, in specific design described herein, structure and method, can carry out various modifications.

Those skilled in the art can obtain various modification of the present invention and application under the prerequisite that does not break away from essence spirit of the present invention and scope. Should be appreciated that to the invention is not restricted to the embodiment that this paper describes in exemplary mode, and should comprise all equivalents.

Claims (231)

1. energy conversion system comprises:

Oxidant delivery system with entrance and exit, it is configured to deliver into described energy conversion system with containing oxidant fluid;

Fuel delivery system, it is configured to deliver into described energy conversion system with containing fuel fluid;

The diluent induction system, it is configured to carry in described energy conversion system and contains the diluent fluid, and wherein at least part of described diluent fluid that contains comprises vaporizable diluent fluid, and at least part of diluent fluid that contains pressurizes into liquid;

Combustion system, it is configured to receive fluid from described fuel delivery system, described oxidant delivery system and described diluent induction system; And comprise the combustion chamber, described combustion chamber has at least one and exports the entrance that exists fluid to be communicated with described oxidant delivery system outlet and described fuel delivery system; Has at least one outlet, described combustion system is configured to mix containing fuel fluid and containing oxidant fluid, to form flammable fuel and oxidant mixture, thereby and with oxidant fuel is carried out oxidation and form oxidation product, and at least part of liquid state is contained the diluent fluid deliver into described combustion chamber; Described combustion system also is configured to and will contains the diluent fluid and contain oxidant fluid, contain a kind of and multiple the mixing and conveying among fuel fluid and the oxidation product; Leave the peak temperature of the high-energy fluid of described combustion system with restriction; And formation comprises the high-energy fluid of the diluent fluid of oxidation product and vaporization in described combustion system, and has one or more level to raise among the temperature of described high-energy fluid, pressure and the kinetic energy;

The expansion system that comprises the decompressor with entrance and exit, it is configured to make at least part of described high-energy fluid to expand, thereby forms expansion fluid;

Have heat and the quality transmission system of a plurality of entrance and exits, it is configured to: thus from described expansion fluid, reclaim the expansion fluid that heat forms cooling; Thereby provide heat to form the diluent fluid of heating to containing the diluent fluid; Be delivered to the diluent fluid of the heating of small part to described combustion system;

The diluent recovery system, it is configured to reclaim diluent from described expansion fluid, and described yield is at least about equaling to be conveyed into the oxidant fluid of described expansion system outlet upstream or the amount in the high-energy fluid; And recovery section water, described water be following both one of or both combinations: the water that forms in the combustion process and together be conveyed into the water of described oxidant delivery system with described oxidant fluid; And

The fluid treatment system, it is configured to removing from least a portion of the water of described expansion fluid recovery, wherein remove the part of at least a alloy in the described expansion fluid, and reduce the concentration of this alloy of the high-energy fluid that enters described expansion system.

2. energy conversion system according to claim 1, the high-energy fluid of wherein said cooling also comprises a small amount of pollutant of at least one class, and described pollutant is by containing fuel fluid, containing oxidant fluid and the reaction that contains between two or more components in the diluent fluid forms; Described energy conversion system be configured to will leave the concentration with at least a pollutant in the fluid of crossing of described energy conversion system be controlled at and be lower than formulation concentration.

3. energy conversion system according to claim 2, also configuration is used for rate of discharge with described a small amount of pollutant and is controlled at and is lower than every generations 1MWh power and discharges the 1kg pollutant.

4. energy conversion system according to claim 1, comprise that configuration is used for controlling the burner of the spatial temperature distribution in the described high-energy fluid, wherein at least one horizontal direction in the burner cross section distributes to the transverse temperature of the described high-energy fluid that leaves described combustion system and controls, and described burner cross section is near described burner outlet.

5. energy conversion system according to claim 1, comprise that configuration is used for controlling the burner of the spatial temperature distribution in the described high-energy fluid, wherein simultaneously the first and second horizontal directions in the burner cross section distribute to the temperature of the described high-energy fluid that leaves described combustion system and control, and described burner cross section is near described burner outlet.

6. energy conversion system according to claim 5, comprise that configuration is used for controlling the burner of the spatial temperature distribution in the described high-energy fluid, wherein the diluent in the described burner and the spatial distribution that contains the fuel fluid conveying are controlled, thereby so that substantially inhomogeneous along the temperature distribution of described the first horizontal direction in the burner cross section, described burner cross section is near described burner outlet.

7. energy conversion system according to claim 1, comprise that configuration is used for controlling the burner of the spatial temperature distribution in the described high-energy fluid, wherein the diluent in the described burner and the spatial distribution that contains the fuel fluid conveying are controlled, thereby so that substantially inhomogeneous along the temperature distribution of described the first horizontal direction in the burner cross section, described burner cross section is near described burner outlet.

8. energy conversion system according to claim 1 comprises that configuration is used for controlling the burner of the spatial temperature distribution in the described high-energy fluid, the transverse temperature that wherein will leave described combustion system distribute be controlled at required transverse temperature and distribute+/-the 10K degree.

9. energy conversion system according to claim 1 wherein is controlled at the cross direction profiles of the ratio of actual outlet temperature and required outlet temperature in required horizontal ratio distributes.

10. energy conversion system according to claim 9 wherein remains on 0.93-1.07 with described temperature ratio.

11. energy conversion system according to claim 9 wherein remains on 0.97-1.03 with described temperature ratio.

12. energy conversion system according to claim 9 wherein will remain on 0.99-1.01 near the temperature ratio in peak temperature zone.

13. energy conversion system according to claim 9, wherein approaching peripheral temperature ratio is 1.00-1.06 with the ratio that connects paracentral temperature ratio.

14. energy conversion system according to claim 1, wherein the uncertainty that describedly contains fuel fluid, contains flow in diluent fluid and the oxidant fluid logistics is controlled at selected scope, thereby define the temperature uncertainty, thereby the peak temperature that leaves the high-energy fluid of described combustion system is lower than designed peak temperature with certain probability in selected temperature uncertainty numerical value, described probability is positioned at required probable range, thereby improves the efficient of described system.

15. energy conversion system according to claim 1, wherein the conveying that contains the diluent fluid is controlled, thereby when abundant premixed, the concentration of leaving the described diluent in the high-energy fluid of described combustion system is higher than the limit of combustibility of these fluids.

16. energy conversion system according to claim 1, wherein said oxidant delivery system also comprises the fluid pressue device, it is configured to the described oxidant fluid that contains is pressurizeed, and wherein enters the pressure of described burner and the pressure ratio of ambient pressure and is higher than about 20.

17. energy conversion system according to claim 16 also is configured to cool off the compressed described oxidant fluid that contains with containing the diluent fluid.

18. energy conversion system according to claim 16 also is configured to the part that contains the diluent fluid from the heating of the second heat exchanger is conveyed into the compressed described oxidant fluid that contains.

19. energy conversion system according to claim 28 also comprises the recompression machine, its configuration is used for described expansion fluid is compressed to and equals at least ambient pressure, and with its discharging.

20. energy conversion system according to claim 19 wherein is configured in described recompression machine the downstream of diluent recovery system.

21. energy conversion system according to claim 19, wherein always unite expansion ratio and be higher than approximately 37, described total associating expansion ratio is the result of pressure ratio of fluid recompression machine of expansion fluid of the cooling in the pressure ratio of the fluid pressue device that contains oxidant fluid of upstream, the described combustion chamber of one or more compressions and the described diluent recovery system of compression downstream.

22. energy conversion system according to claim 28, wherein control the mass flow and the ratio that contains the mass flow of oxidant fluid of condensable diluent, thereby described energy conversion system with respect to the clean specific power that contains the oxidant fluid total flow be higher than 940kW/ (kg/s) (=kJ/kg) leave the compression the described fluid flow that contains the fluid compression device of oxidant fluid, described clean specific power comprises that the general power of described decompressor deducts be used to compressing the summation of power of expansion fluid that describedly contains oxidant fluid, contains the cooling in fuel fluid and diluent fluid and described diluent recovery system downstream, and wherein said oxidant is air.

23. energy conversion system according to claim 28, wherein control the mass flow and the ratio that contains the mass flow of oxidant fluid of condensable diluent, thereby when air is operated, described energy conversion system with respect to the clean specific power of described decompressor flow be higher than 700 kW/ (kg/s) (=kJ/kg) enter the fluid flow of described decompressor, described clean specific power comprises that the general power of described decompressor deducts be used to compressing the summation of power of expansion fluid that describedly contains oxidant fluid, contains the cooling in fuel fluid and diluent fluid and described diluent recovery system downstream.

24. energy conversion system according to claim 1, the pressure decreased of expansion fluid of cooling that wherein said recompression fluid pressue device is configured to leave described diluent recovery system is for lower by 1% than ambient pressure at least, and wherein said recompression fluid pressue device is used for compressing the expansion fluid of the cooling in described diluent recovery system downstream.

25. energy conversion system according to claim 24, wherein said recompression machine also are configured to change ambient pressure to the recompression ratio of the expansion fluid pressure of described cooling.

26. energy conversion system according to claim 1, the compression ratio of described fluid pressue device of expansion fluid that wherein will compress the cooling in described diluent recovery system downstream is configured to 1.1-8.

27. energy conversion system according to claim 1, also be configured to control condensable diluent in the described high-energy fluid to the temperature of the expansion fluid of the ratio of condensable gases not, described cooling to external world ratio, and the described recompression ratio of temperature, thereby the concentration of leaving the diluent fluid in the fluid of described energy conversion system is lower than desired saturated concentration ratio, thereby control forms the probability of the column of smoke.

28. energy conversion system according to claim 1, also comprise the decompressor with entrance and exit, it is configured to make described high-energy fluid to expand into the lower pressure that described decompressor exports by the elevated pressures of described decompressor entrance, and wherein said decompressor entrance exists fluid to be communicated with described burner.

29. energy conversion system according to claim 28, wherein said decompressor is working machine, and it is configured to energy contained in the described high-energy fluid is converted to useful mechanical energy.

30. energy conversion system according to claim 28 is wherein carried described fluid and expansion ratio is configured and controls, thereby makes the outlet temperature of the fluid that leaves described decompressor be lower than 500 degrees centigrade.

31. energy conversion system according to claim 28, also dispose and setting is used for controlling described fluid and carries and expansion ratio, thereby the diluent concentration that leaves the high-energy fluid of described decompressor is lower than described saturated concentration, thereby diluent can condensation in described decompressor.

32. energy conversion system according to claim 29 also comprises the generator that is mechanically connected to described decompressor, it is configured at least part of described mechanical energy is converted to mechanical energy.

33. energy conversion system according to claim 32, wherein said heat and quality transmission system also comprise heat exchanger, and it is configured to contain the diluent fluid from described generator recovery heat and heating.

34. energy conversion system according to claim 33 also is configured to control the flow that contains the diluent fluid of described generator heat exchanger of flowing through, and the temperature of described generator remained on is lower than desired level.

35. energy conversion system according to claim 33 also is configured to cool off described generator with low viscosity fluid, and with the described diluent fluid heat-shift that contains.

36. energy conversion system according to claim 33, the fluid that also is configured to comprise from least part of and described decompressor outlet upstream of the diluent of the heating of the heat of described generator mixes.

37. energy conversion system according to claim 29, also comprise the decompressor driver that described decompressor is linked to each other with machine applications, and described heat and quality transmission system also comprise heat exchanger, and this heat exchanger is configured to from what described decompressor driver reclaimed heat and carried heating contain the diluent fluid.

38. described energy conversion system according to claim 37 also is configured to temperature with described driver lubricant and remains on and be lower than required temperature.

39. energy conversion system according to claim 1 also comprises:

Generator, motor, electromagnetic transducer and electromagnetic controller that heat generating component, one or more and described decompressor link to each other;

And described heat and quality transmission system also comprise the component heat interchanger, and this heat exchanger is configured to control the flow that contains the diluent fluid, wherein control the temperature of described heat generating component and heat is recycled to containing in the diluent fluid of heating.

40. described energy conversion system also is configured to control the flow that contains the diluent fluid according to claim 39, is lower than 100 degrees centigrade thereby the temperature of described electric transducer remained on.

41. energy conversion system according to claim 28 also comprises at least the second decompressor, it is configured to extract power from described high-energy fluid, and the power of its extraction surpasses 1.5 times of power that described the first expansion function extracts under design condition.

42. energy conversion system according to claim 1 wherein disposes described controller and controls described fluid and carry, thereby the temperature that will enter the high-energy fluid of described decompressor is controlled at and is no more than required temperature.

43. energy conversion system according to claim 1 also comprises the fuel treatment system that exists fluid to be communicated with described diluent induction system, its be configured to process described contain fuel fluid and it be delivered to described energy conversion system use.

44. described fuel treatment system also comprises cleaning device according to claim 43, it is configured to be removed to the described alloy that contains in the fuel fluid of small part.

45. described fuel treatment system also is configured to from the described alloy that filters out the fuel fluid greater than required size that contains according to claim 44.

46. energy conversion system according to claim 1, wherein from the heat of the high-energy fluid in described decompressor downstream with just be transported to described combustion system contain the fuel fluid heat exchange.

47. energy conversion system according to claim 1 wherein remained on the described temperature that contains fuel fluid before being conveyed into described combustion system and is lower than required temperature, carried with the fuel fluid that contains that basic maintenance is required.

48. described energy conversion system is controlled described recuperation of heat according to claim 47, is lower than 100 degrees centigrade thereby before being conveyed into described combustion system the described temperature that contains fuel fluid remained on.

49. energy conversion system according to claim 1 also comprises the diluent treatment system that exists fluid to be communicated with described diluent induction system, it is configured to process described diluent to be used for described energy conversion system.

50. described diluent treatment system also comprises cleaning device according to claim 49, its configuration is used for being removed to the described part alloy that contains in the diluent fluid of small part.

51. described diluent treatment system also is configured to filter out at least part of described alloy greater than required size that contains in the diluent fluid according to claim 50.

52. described diluent treatment system also is configured to removing the described at least part of solvable alloy that contains in the diluent fluid according to claim 50.

53. described diluent treatment system also is configured to remove the diluent that part reclaims from described energy conversion system according to claim 49.

54. 3 described diluent treatment systems according to claim 5, also be configured to from described energy conversion system, remove the part diluent, thereby remove at least a portion of at least a alloy from described energy conversion system, the concentration that wherein enters this alloy of described decompressor to the major general remains on and is lower than desirable value.

55. described diluent treatment system according to claim 49, also be configured at least part of concentration that contains the diluent component of diluent fluid is reduced to and be lower than desirable value, wherein when this diluent at least part of being delivered to described decompressor outlet upstream, the concentration that is delivered to this component in the high-energy fluid of described decompressor is lower than desired concn.

56. energy conversion system according to claim 1 also is configured to the diluent that part reclaims is recycled to the upstream that described combustion system exports.

57. 6 described energy conversion systems according to claim 5 are configured to reduce the part alloy of the diluent that part reclaims.

58. 7 described energy conversion systems also are configured to the described diluent of abundant purifying according to claim 5, thereby the total concentration that comprises at least a alloy in the high-energy fluid of recovery diluent of this purifying is lower than desired level.

59. energy conversion system according to claim 1 also comprises the diluent recovery system, it is configured to recovery section diluent from the described fluid of using.

60. 9 described diluent treatment systems also are configured to control the diluent part of removing from described energy conversion system according to claim 5, wherein control the dilution dosage in the described energy conversion system.

61. 9 described diluent recovery systems also are configured to recovery section diluent from the described fluid of using according to claim 5, the part that reclaims equals to be delivered to the part of described decompressor outlet upstream at least.

62. 1 described diluent recovery system according to claim 6, also be configured to the recovery section diluent, the part that reclaims is equal to or greater than the diluent that is delivered to described decompressor outlet upstream and partly adds the diluent part that need remove from described energy conversion system.

63. 9 described energy conversion systems according to claim 5, also be configured to recovery section diluent from the described fluid of using, the part that the part that reclaims equals can to carry described decompressor outlet upstream adds that the diluent that forms in the combustion process partly adds the relative humidity part that oxidant fluid receives that contains by input.

64. energy conversion system according to claim 1 is configured to make water as the described diluent that contains in the diluent fluid.

65. energy conversion system according to claim 1, wherein said diluent recovery system comprises the direct contact type condenser.

66. 5 described energy conversion systems according to claim 6 wherein enter the cooling agent fluid of described diluent recovery system and the temperature difference left between the temperature of high-energy fluid of cooling of described diluent recovery system is lower than 20K (36 °F).

67. 5 described energy conversion systems according to claim 6 wherein enter the cold diluent fluid of described diluent recovery system and the temperature difference left between the temperature of high-energy fluid of cooling of described diluent recovery system is lower than 4K (7.2 °F).

68. energy conversion system according to claim 1, wherein said diluent recovery system are also removed the filtrable alloy of part from the expansion high-energy fluid of described cooling.

69. energy conversion system according to claim 1, wherein said diluent recovery system are also removed partly soluble alloy from the high-energy fluid of the expansion of described cooling.

70. energy conversion system according to claim 1, also comprise the first heat exchanger with hotter entrance and colder outlet, it is used for the high-energy fluid of at least part of described expansion and at least part of diluent fluid that contains are carried out the heat exchange, and wherein said hotter entrance exists fluid to be communicated with described decompressor outlet.

71. 0 described energy conversion system according to claim 7, wherein the part with the diluent of heating is delivered to described combustion system.

72. energy conversion system according to claim 1 also comprises the diluent recovery system that exists fluid to be communicated with described decompressor outlet, its configuration is used for reclaiming the diluent fluid.

73. 2 described diluent recovery systems are configured to reclaim required at least part diluent from the fluid of using that leaves described decompressor according to claim 7.

74. 2 described energy conversion systems are configured at least part of diluent fluid that reclaims is recycled in described energy conversion system according to claim 7.

75. 0 described energy conversion system according to claim 7, wherein said heat exchanger is positioned at the downstream of decompressor.

76. 5 described energy conversion systems also are configured to reclaim at least part of diluent fluid from described expansion fluid according to claim 7.

77. 6 described energy conversion systems according to claim 7, wherein the diluent fluid that contains with at least part of described heating is delivered to described combustion system.

78. energy conversion system according to claim 1 wherein mixes the described diluent of part with the fuel fluid that contains of combustion process upstream.

79. energy conversion system according to claim 1 wherein mixes the described diluent of part with the oxidant fluid that contains of combustion process upstream.

80. energy conversion system according to claim 1 also comprises the second heat exchanger that is positioned at described the first heat exchanger downstream, thereby so that described high-energy fluid is cooled off at least part of described high-energy fluid and at least part of colder diluent heat exchange.

81. energy conversion system according to claim 1, wherein said heat and quality transmission system also comprise the second heat exchanger that is positioned at described the first heat exchanger downstream.

82. 1 described energy conversion system wherein is configured described heat and quality transmission system according to claim 8, thereby the area of described the second heat exchanger is 20%-150% to the ratio of the area of described the first heat exchanger.

83. 1 described energy conversion system wherein reclaims heat by liquid diluent from the expansion fluid of described downstream the second heat exchange of flowing through according to claim 8.

84. 1 described energy conversion system according to claim 8, wherein the liquid diluent that heats in the second heat exchanger of described downstream of transport portion cools off by the oxidant fluid that contains of described oxidant fluid pressue device compression.

85. 1 described energy conversion system comprises that also configuration is used for controlling the device that is delivered to hot diluent mass flow described the first heat exchanger and that be delivered to described oxidant delivery system from described the second heat exchanger according to claim 8.

86. 1 described energy conversion system according to claim 8, also comprise disposing to be used for controlling being delivered to described oxidant delivery system entrance from described the second heat exchanger, and enter the device that contains the hot diluent mass flow in the oxidant fluid of the compression in the described oxidant delivery system.

87. energy conversion system according to claim 1, the liquid diluent stream part that wherein is delivered to the heating of described oxidant fluid pressue device are less than or equal to make the saturated required amount of oxidant fluid that contains of leaving described oxidant compression system.

88. energy conversion system according to claim 1, wherein said heat and quality transmission system also comprise the condensation heat recovery system that is positioned at described the first heat exchanger downstream, and it uses cooling agent fluid to reclaim heat from the high-energy fluid of at least part of diluent fluid condensation that is enough to make at least part of described vaporization.

89. energy conversion system according to claim 1, wherein said heat and quality transmission system also comprise cooling system, are used for the diluent condensation of cooling off the cooling agent of described expansion fluid and making described vaporization with cooling.

90. comprising, 9 described energy conversion systems according to claim 8, wherein said condensation heat recovery system use diluent as the direct heat exchanger of cooling agent fluid.

91. 0 described energy conversion system according to claim 9, wherein described direct contact type heat and quality transmission system and described cooling agent diluent mass flow are configured, thereby leave the temperature difference between the cooling agent diluent of the fluid of using of cooling of described direct heat exchanger and described heating less than 4 degrees centigrade.

92. energy conversion system according to claim 1, wherein said heat and quality transmission system comprise the 3rd heat exchanger that is positioned at described decompressor downstream and described the first heat exchanger upstream, to reclaim heat and heats coolant fluid from described expansion fluid.

93. 2 described energy conversion systems comprise that also configuration is used for controlling the device that is delivered to hot diluent mass flow described the second heat exchanger and that be delivered to described oxidant delivery system from described the first heat exchanger according to claim 9.

94. 2 described energy conversion systems according to claim 9, wherein said cooling agent fluid comprises the liquid heat diluent, and at least part of described hot diluent evaporates in described the 3rd heat exchanger.

95. 2 described energy conversion systems according to claim 9, wherein said cooling agent fluid is hot diluent, and at least part of described hot diluent evaporates in described the 3rd heat exchanger and further heating to form overheated diluent.

96. 2 described energy conversion systems according to claim 9, the cooling agent side of wherein said described the 3rd heat exchanger exists fluid to be communicated with the combustion system that is positioned at described compressor downstream and described decompressor upstream.

97. 2 described energy conversion systems according to claim 9, wherein the diluent with described the 3rd heat exchanger heating mixes with the fluid of the combustion system that is arranged in described oxidant compressor downstream and described decompressor upstream.

98. 2 described energy conversion systems according to claim 9, wherein the diluent with described the 3rd heat exchanger heating mixes with the fluid that is positioned at described burning starting point upstream.

99. energy conversion system according to claim 1, wherein said heat and quality transmission system also comprise the backheat heat exchanger, it is configured to reclaim heat from the expansion fluid that leaves described decompressor, and heats the oxidant fluid that contains of described combustion system upstream.

100. 9 described energy conversion systems wherein are configured described heat and quality transmission system according to claim 9, thereby the long-pending ratio with described diluent heat exchanger of the heat recovery surface of described backheat heat exchanger is 20%-300%.

101. 9 described energy conversion systems according to claim 9, wherein described heat and quality transmission system are configured, thereby the expansion fluid part of carrying the heat exchanger by described decompressor downstream is identical with the expansion fluid part of carrying the backheat heat exchanger that contains oxidant fluid by heating described combustion system upstream.

102. the system as claimed in claim 1, wherein said fluid treatment system also disposes to process described diluent fluid, describedly contains fuel fluid and describedly contain in the oxidant fluid one or more, enters the concentration of at least one component of the high-energy fluid of described expansion system with reduction.

103. at least two entrances and at least one outlet that heat and quality transmission system, conversion are used for being connected with energy conversion system, wherein said heat and quality transmission system comprise:

Oxidant delivery system, it is configured to be delivered to described energy conversion system with containing oxidant fluid;

Fuel delivery system, it is configured to be delivered to described energy conversion system with containing fuel fluid;

The diluent induction system, its diluent fluid that contains that is configured to comprise the diluent fluid of can vaporizing directly injects described energy conversion system;

The combustion system that comprises the combustion chamber, it is configured to make, and part is described contains that diluent fluid and part are described to contain the oxidant fluid reaction, and the evaporation part divides described liquid diluent to form high-energy fluid;

The expansion system that comprises at least one expansion gear, it is configured to make at least part of described high-energy fluid to expand and produces expansion fluid;

Heat exchanger, it is configured to make at least part of described expansion fluid and at least part of described diluent fluid heat exchange that contains; And

Be positioned at the heat recovery system in described heat exchanger downstream, it is configured to reclaim heat with the fluid of formation cooling from least part of described expansion fluid, and reclaims thus the diluent of the described energy conversion system of at least part of injection;

Wherein said heat and quality transmission system reclaim following at least a key element: at least part ofly will and at least part of described heat be converted to useful mechanical power with the heat of high-energy fluid discharging, other heats with this fluid in using with the fluid of at least part of heating and at some, and at least part of described diluent fluid, at least part of described cooling agent fluid and at least part of water that is formed by oxidizing process.

104. according to claim 10 3 described heats and quality transmission system, wherein said expansion system comprise at least one recompression device, it is configured to described expansion fluid is recompressed.

105. according to claim 10 3 described heats and quality transmission system, wherein said combustion system is heat insulation, thereby reduces the heat loss of described combustion system.

106. according to claim 10 3 described heats and quality transmission system, wherein said combustion system comprises heat-proof device, and it is configured to reduce the heat that described combustion system assembly obtains from one of described combustion process and described high-energy fluid.

107. according to claim 10 3 described heats and quality transmission system, wherein said combustion system comprises at least one radiation shield, and it is configured to tackle from least a radiation in described burning fluid and the described high-energy fluid.

108. according to claim 10 3 described heats and quality transmission system, wherein said combustion system also comprises cooling system.

109. according to claim 10 8 described heats and quality transmission system, wherein said cooling system comprise be used to the fluid and the device that carries out the surface heat exchange than cold fluid that is supplied to described cooling system that make in the described combustion chamber.

110. according to claim 10 8 described heats and quality transmission system, wherein said cooling system comprise be used to the fluid and the device that carries out the direct contact type heat exchange than cold fluid that is supplied to described cooling system that make in the described combustion chamber.

111. according to claim 10 3 described heats and quality transmission system, wherein said heat and quality transmission system contain the diluent fluid with part and are delivered to described oxidant delivery system, be used for subsequently the described diluent fluid that contains being returned described heat and quality transmission system by the described oxidant fluid that contains of heat-exchange device cooling.

112. according to claim 10 3 described heats and quality transmission system, wherein said heat and quality transmission system contain the diluent fluid with part and are delivered to described oxidant delivery system, be used for subsequently the described diluent fluid that contains being returned described heat and quality transmission system by the described oxidant fluid that contains of surface heat switch cooling.

113. according to claim 11 1 described heat and quality transmission system, wherein said heat-exchange device are positioned at the upstream of recompression device.

114. according to claim 10 3 described heats and quality transmission system, wherein said heat and quality transmission system contain the diluent fluid with part and are delivered to described oxidant delivery system, are used for mixing with at least part of oxidant fluid that contains by the fluid mixing arrangement in the described oxidant delivery system.

115. according to claim 11 4 described heats and quality transmission system, wherein said mixing arrangement is positioned at before or after any described compression set.

116. according to claim 11 4 described heats and quality transmission system, wherein said mixing arrangement directly injects at least one described compression set with the described diluent fluid that contains of part.

117. according to claim 10 3 described heats and quality transmission system wherein are cooled to the oxidant fluid that contains in the described oxidant delivery system of small part by cooling device.

118. according to claim 11 7 described heats and quality transmission system, wherein said cooling device is positioned at before or after any described compression set.

119. according to claim 10 3 described heats and quality transmission system, wherein said oxidant delivery system is supplied to described heat and quality transmission system to be used for further processing at least part of described oxidant fluid that contains.

120. 3 described heats and quality transmission system also comprise at least one heat exchanger on the heat generating component of at least one in being selected from generator, turbine generator driver and electric transducer according to claim 10, wherein said heat generating component is cooled.

121. according to claim 12 0 described heat and quality transmission system, wherein said heat generating component are contained the cooling of diluent fluid.

122. according to claim 10 3 described heats and quality transmission system, wherein said fuel delivery system contain fuel fluid with part and are supplied to described heat and quality transmission system to be used for further processing.

123. according to claim 10 3 described heats and quality transmission system, wherein said diluent induction system contain the diluent fluid with part and are supplied to described heat and quality transmission system to be used for further processing.

124. 3 described heats and quality transmission system also are configured to the described oxidant fluid that contains of part is delivered to described combustion chamber according to claim 10.

125. 3 described heats and quality transmission system also are configured to the described fuel fluid that contains of part is delivered to described combustion chamber according to claim 10.

126. 3 described heats and quality transmission system also are configured to the described diluent fluid that contains of part is delivered to described combustion chamber according to claim 10.

127. according to claim 10 9 described heats and quality transmission system also are configured to a part with some fluid and are delivered to cooling system in the described combustion system, this fluid returns described heat and quality transmission system thereafter.

128. according to claim 10 3 described heats and quality transmission system, also be configured to the described diluent fluid that contains of part is delivered to described expansion system, expansion fluid for cooling off by surface heat exchanger in the described expansion system returns the described diluent fluid that contains to described heat and quality transmission system thereafter.

129. according to claim 11 1 described heat and quality transmission system, wherein said heat-exchange device is positioned at the downstream of described expansion gear and the upstream of described recompression device.

130. according to claim 11 1 described heat and quality transmission system, wherein said heat-exchange device is positioned at the downstream of described recompression device.

131. according to claim 10 3 described heats and quality transmission system, wherein said heat and quality transmission system are delivered to described expansion system with the described diluent fluid that contains of part, are used for mixing with some fluid by the fluid mixing arrangement of described expansion system.

132. according to claim 13 1 described heat and quality transmission system, wherein said mixing arrangement are positioned at before or after any described expansion gear or the recompression device.

133. according to claim 13 1 described heat and quality transmission system, wherein said mixing arrangement directly injects at least one described expansion gear or recompression device with the described diluent fluid that contains of part.

134. 3 described heats and quality transmission system are wherein cooled off some fluid in the described expansion system of part by some cooling devices according to claim 10.

135. according to claim 13 4 described heats and quality transmission system, wherein said cooling device are positioned at before or after any described expansion gear or the recompression device.

136. 3 described heats and quality transmission system are wherein processed at least part of described heat and quality transmission system of being supplied to of some fluid in the described expansion system for further according to claim 10.

137. according to claim 10 3 described heats and quality transmission system, wherein said heat and quality transmission system are delivered to described expansion system with the part of some fluid.

138. according to claim 10 3 described heats and quality transmission system, wherein said energy conversion system comprises at least one pump.

Contain diluent fluid and/or coolant flow body and be used for cooling off at least one pump in the described energy conversion system 139. according to claim 10 3 described heats and quality transmission system, wherein said heat and quality transmission system are delivered to small part.

140. according to claim 10 3 described heats and quality transmission system, wherein said heat and quality transmission system are delivered to environment or other process with at least part of heat.

141. according to claim 10 3 described heats and quality transmission system, wherein said heat and quality transmission system contain the diluent fluid with part and are delivered to environment or other process.

142. according to claim 10 3 described heats and quality transmission system, wherein said heat and quality transmission system are delivered to described energy conversion system outer environment or other process with partial discharge gas.

143. according to claim 10 3 described heats and quality transmission system, wherein said heat and quality transmission system are delivered to other outer process of described energy conversion system with the part hot fluid.

144. 3 described heats and quality transmission system wherein are used for described hot fluid other outer process of described energy conversion system according to claim 14, subsequently its at least a portion are returned described heat and quality transmission system.

145. according to claim 14 3 described heats and quality transmission system, wherein said hot fluid be vaporization contain the diluent fluid.

146. being the liquid state of heat, according to claim 14 3 described heats and quality transmission system, wherein said hot fluid contain the diluent fluid.

147. 3 described heats and quality transmission system wherein provide energy with described hot fluid to process of refrigerastion according to claim 14.

148. according to claim 10 3 described heats and quality transmission system are wherein by using the surface heat switch with described discharging gas or the described liquid state of part is contained the diluent fluid to high energy gas or described cooling agent fluid heats.

149. according to claim 14 8 described heats and quality transmission system, wherein with at least part of described heating contain the diluent fluid or described cooling agent fluid directly injects described combustion chamber.

150. according to claim 14 8 described heats and quality transmission system, wherein with at least part of described heating contain the diluent fluid or described cooling agent fluid cools off the described oxidant fluid that contains.

151. according to claim 14 8 described heats and quality transmission system, wherein with at least part of described heating contain the diluent fluid or described cooling agent fluid heats described fuel by the surface heat switch, wherein this fuel is transported to described combustion chamber.

152. according to claim 14 8 described heats and quality transmission system, wherein with some mixing arrangements with at least part of described heating contain the diluent fluid or described cooling agent fluid mixes with described fuel, wherein said fuel is transported to described combustion chamber.

153. according to claim 14 8 described heats and quality transmission system are wherein mixed with the described fuel of part with the diluent fluid that contains of some mixing arrangements after with at least part of described evaporation, wherein said fuel is transported to described combustion chamber.

154. according to claim 15 3 described heats and quality transmission system wherein at least part ofly describedly contain the fuel fluid vaporization, and wherein at least part of described fuel fluid that contains is transported to described combustion chamber.

155. according to claim 10 3 described heats and quality transmission system, wherein with at least part of described heating contain the diluent fluid or described coolant flow body is used for the outer heating process of described energy conversion system.

156. 3 described heats and quality transmission system wherein make at least part of described liquid state contain the diluent flow evacuator body by some surface heat switches with described discharging gas or high energy gas according to claim 10.

157. 6 described heats and quality transmission system are wherein directly injected described combustion chamber with the diluent fluid that contains after at least part of described evaporation according to claim 15.

158. according to claim 15 6 described heats and quality transmission system are wherein with the heating process that the diluent flow body is used for the outer needs vaporization fluid of described energy conversion system that contains after at least part of described evaporation.

159. 8 described heats and quality transmission system wherein will be returned described heat and quality transmission system at least a portion that contains the diluent fluid of the heating process that needs the vaporization fluid according to claim 15.

160. 6 described heats and quality transmission system wherein are used for the diluent flow body that contains after at least part of described evaporation to contain fuel fluid at the surface heat exchanger heating part according to claim 15, wherein the described fuel of part is transported to described combustion chamber.

161. according to claim 10 3 described heats and quality transmission system wherein contain the diluent fluid by surface heat exchanger with what described discharging gas or high energy gas further were heated to the described vaporization of small part.

162. according to claim 16 1 described heat and quality transmission system, wherein the diluent fluid that contains with at least part of described further heating directly injects described combustion chamber.

163. according to claim 16 1 described heat and quality transmission system are wherein with the heating process that the diluent flow body is used for the outer needs vaporization fluid of described energy conversion system that contains of at least part of described further heating.

164. 3 described heats and quality transmission system wherein will be returned described heat and quality transmission system at least a portion that contains the diluent fluid of the heating process that needs the vaporization fluid according to claim 16.

165. according to claim 16 1 described heat and quality transmission system, wherein the diluent flow body that contains with at least part of described further heating is used for being heated to the described fuel fluid that contains of small part by some surface heat exchangers, and wherein the described fuel fluid that contains of part is transported to described combustion chamber.

166. 1 described heat and quality transmission system are wherein mixed with the described fuel fluid that contains of part with the diluent fluid that contains of some mixing arrangements with at least part of described heating according to claim 16, wherein said fuel is transported to described combustion chamber.

167. 6 described heats and quality transmission system wherein at least part of described fuel fluid that contains is vaporized, and wherein at least part of described fuel fluid that contains are transported to described combustion chamber according to claim 16.

168. according to claim 10 3 described heats and quality transmission system are wherein by using the surface condensation device that the gaseous state of the described high-energy fluid of part or partial discharge is contained at least part of diluent fluid or water condensation of containing in the diluent fluid.

169. according to claim 10 3 described heats and quality transmission system are wherein by using direct fluid contacting apparatus to contain from the gaseous state of the described high-energy fluid of part or partial discharge that condensation goes out at least part of diluent fluid or water of containing the diluent fluid.

170. 8 and 169 described heats and quality transmission system are wherein passed through the described cooling fluid of part with the described high-energy fluid of part or are discharged air cooling but according to claim 16.

171. 0 described heat and quality transmission system wherein remove heat by cooling device from least part of described cooling fluid according to claim 17, and use subsequently pump or other EGR that described cooling fluid is recycled with further cooling.

172. according to claim 17 1 described heat and quality transmission system, wherein with at least part of described condensation and reclaim contain the diluent fluid or water is recycled to described cooling device.

173. according to claim 17 1 described heat and quality transmission system wherein are used for other purposes in described heat and the quality transmission system with at least part of described condensation and contain diluent fluid or the water that reclaim.

174. according to claim 17 1 described heat and quality transmission system, wherein with at least part of described condensation and reclaim contain the diluent fluid or water is used for described heat and the outer heating process of quality transmission system.

175. 1 described heat and quality transmission system wherein will be returned described heat and quality transmission system for the part that contains the diluent fluid of the heating process outside described heat and the quality transmission system according to claim 17.

176. require described heat and quality transmission system according to right 171, wherein with at least part of described condensation and reclaim contain the diluent fluid or water is discharged described energy conversion system.

177. 0 described heat and quality transmission system wherein are used at least part of described cooling fluid the various uses in described heat and the quality transmission system according to claim 17.

178. 0 described heat and quality transmission system wherein are used at least part of described cooling fluid described heat and the outer heating process of quality transmission system according to claim 17.

179. 8 described heats and quality transmission system wherein will be returned described heat and quality transmission system for the part that contains diluent fluid or water of the heating process outside described heat and the quality transmission system according to claim 17.

180. 8 and 169 described heats and quality transmission system wherein will be left the high energy gas of described condensing unit or the part of discharging gas and discharge described energy conversion system according to claim 16.

181. according to claim 16 8 and 169 described heats and quality transmission system, the part that wherein will leave the high energy gas of described condensing unit or discharging gas is delivered to a recompression machine in the described exhaust system.

182. according to claim 10 3 described heats and quality transmission system are configured to be heated to the described oxidant fluid that contains of small part by surface heat exchanger with the expansion fluid of the described expansion fluid of part or cooling.

183. according to claim 10 3 described heats and quality transmission system, wherein make at least part of described oxidant stream that contains in fluid contacting apparatus, describedly contain the diluent fluid or the described cooling agent fluid of part contacts with at least part of, at least part ofly in this device describedly contain the diluent fluid or the described coolant flow evacuator body of part enters the described oxidant fluid that contains.

184. according to claim 10 3 described heats and quality transmission system also comprise at least one configuration be used for circulating device of at least a described fluid.

185. according to claim 10 3 described heats and quality transmission system comprise that also at least one configuration is used for the pressure of at least a described fluid is brought up to the device of higher value.

186. 3 described heats and quality transmission system comprise that also at least one configuration is used for the pressure decreased of at least a described fluid is arrived the more device of low value according to claim 10.

187. the method that the heat in the control energy conversion system and quality are transmitted, described energy conversion system comprises:

The burner that comprises the combustion chamber, it is configured to receive and contains oxidant fluid, contains fuel fluid and contain the diluent fluid, thereby described combustion chamber is configured to make from described and contains at least part of fuel of fuel fluid and form high-energy fluid from the described at least part of oxidant reaction that contains oxidant fluid, described high-energy fluid comprises product and from describedly containing oxidant fluid, contain fuel fluid and contain the residual components of diluent fluid, and has at least a level higher in its temperature, pressure and the speed;

Oxidant delivery system, it is configured to be delivered to described burner with containing oxidant fluid;

Fuel delivery system, it is configured to be delivered to described burner with containing fuel fluid;

The diluent induction system, its diluent fluid that contains that is configured to comprise the diluent fluid of can vaporizing is delivered to described burner;

The fluid expansion system that comprises at least one expansion gear, it is configured to make the described high-energy fluid of part to expand, thereby forms the high-energy fluid that expands;

Heat and quality transmission system, it comprises at least one heat exchanger and has at least two entrances and an outlet, described heat becomes with the quality delivery system configuration: will carry out heat exchange from heat and the cooling agent fluid of the high-energy fluid of at least part of described expansion, and carry out the quality transmission in described containing in diluent fluid and the described high-energy fluid that contains oxidant fluid, described high-energy fluid and described expansion between at least a fluid;

The control system that comprises controller, it is configured to control: by the fuel fluid that contains of described fuel delivery system conveying, contain the diluent fluid by what described diluent induction system was carried, contain in diluent fluid and the described high-energy fluid that contains oxidant fluid, described high-energy fluid and described expansion quality transmission between at least two kinds of fluids in the described energy conversion system; And the distribution of diluent conveying; Described control method comprises:

Control the conveying that contains fuel fluid in the described combustion system;

Control the conveying that contains oxidant fluid in the described combustion system;

Control containing the diluent fluid and containing in the high-energy fluid of oxidant fluid, high-energy fluid and expansion quality transmission between at least two kinds of fluids in the described energy conversion system; And

Control the distribution that the diluent fluid is carried that contains in the described energy conversion system;

The peak temperature that wherein will leave the high-energy fluid of described burner is controlled at and is lower than predetermined decompressor peak temperature, and reclaims heat from described expansion fluid.

188. such as the described control method of claim 187, comprise that also the diluent of the described expansion system of control upstream is carried.

189. such as the described control method of claim 187, comprise that also the described diluent fluid that contains of control is to the conveying of described oxidant delivery system.

190. such as the described control method of claim 187, comprise that also the described diluent fluid that contains of control is to the conveying of described combustion system.

191. such as the described control method of claim 187, comprise that also control is delivered to the cooling agent fluid of described expansion fluid heat exchanger, wherein heat be recovered into described cooling agent fluid from the high-energy fluid of described expansion.

192. such as the described control method of claim 187, wherein said cooling agent fluid comprises and contains the diluent fluid, what described control method comprised also that control is delivered to described expansion fluid heat exchanger contains the diluent fluid, thereby heat is recovered into described diluent from the high-energy fluid of described expansion.

193. such as the described control method of claim 192, also comprise the temperature of the expansion high-energy fluid of controlling described cooling.

194. such as the described control method of claim 187, described energy conversion system also comprises the diluent recovery system, the described control method of claim 187 comprises that also control is from the diluent part of the high-energy fluid recovery of described expansion.

195. such as the described control method of claim 187, described method comprises also that control comprises and contains the diluent fluid and contain one of them cooling agent fluid of oxidant fluid to the conveying of the described energy conversion system assembly that is heated by described high-energy fluid, wherein the temperature of this assembly is controlled at and is no more than predetermined temperature.

196. such as the described control method of claim 187, the further heat-shift of described method is with the part diluent in the high-energy fluid that reclaims described expansion, thereby form the expansion fluid of cooling and the cooling agent fluid of heating, wherein said cooling agent fluid comprises at least part of diluent.

197. such as the described control method of claim 187, wherein said expansion system also comprises the recompression device, it is configured to, and the high-energy fluid to described cooling recompresses after reclaiming diluent, thereby form the discharging fluid and described discharging fluid is expelled to surrounding environment, described control method also comprises the pressure of the expansion high-energy fluid of controlling the cooling of leaving described recompression device.

198. such as the described control method of claim 197, the pressure of expansion high-energy fluid that also will be positioned at the cooling of described recompression device upstream is controlled at and is higher than about 80% of environmental pressure.

199. such as the described control method of claim 197, the pressure of expansion high-energy fluid that also will be positioned at the cooling of described recompression device upstream is controlled at less than or equal to about 80% of environmental pressure.

200. such as the described control method of claim 187, the wherein said diluent fluid that contains comprises the chemical constituent that can form by described reaction, and described method comprises also that the diluent that the high-energy fluid from described expansion is reclaimed partly is controlled at and is equal to or greater than the dilution dosage that is delivered to described expansion system upstream.

201. such as the described control method of claim 200, wherein said diluent comprises water, and described method comprises also that the diluent that will reclaim from the high-energy fluid of described expansion partly is controlled at and further comprises by what described oxidant delivery system received and contain relative humidity part the oxidant fluid.

202. such as the described control method of claim 200, comprising also that the diluent that will reclaim from the high-energy fluid of described expansion partly is controlled to be comprises that all that received by described oxidant delivery system contain the relative humidity the oxidant fluid, and also comprises the diluent part that described combustion process forms.

203. such as the described control method of claim 202, comprise that also the diluent that the high-energy fluid from described expansion is reclaimed partly is controlled to be the water that comprises that also basically all combustion processes form.

204. such as the described control method of claim 187, wherein said energy conversion system also comprises the electro-heat equipment that comprises heat exchanger, described device is selected from generator, motor, thermo-mechanical drive, pump, bearing, electromagnetic transducer and electromagnetic controller; Wherein

The configuration of described controller is used for controlling the flow of cooling agent diluent fluid of described heat exchanger of flowing through, described control method also comprises the flow of controlling described cooling agent diluent, wherein the temperature of described electro-heat equipment is remained on to be lower than the electro-heat equipment temperature limiting.

205. such as the described control method of claim 204, comprise also that temperature with described electro-heat equipment is controlled at and be lower than about 343 ℃ (650 °F).

206. such as the described control method of claim 204, comprise also that temperature with described electro-heat equipment is controlled at and be lower than about 100 ℃ (212 °F).

207. such as the described control method of claim 187, wherein said energy conversion system also comprises the thermal technology's section that is configured to contact high-energy fluid, and comprises thermal technology's section heat exchanger; It is one of following that described thermal technology's section is selected from: the combustion chamber, contain fuel fluid and carry assembly, flame controller, balance cylinder, turbine blade, turbine stator turbine guard shield,

The configuration of wherein said controller is used for controlling the flow of cooling agent diluent fluid of described heat exchanger of flowing through, described control method also comprises the flow of controlling described cooling agent diluent, wherein the temperature of described thermal technology's section is remained on to be lower than predetermined thermal technology's section temperature limiting.

208. such as the described control method of claim 187, wherein said heat become with the quality delivery system configuration will heating the diluent fluid that contains be delivered to described burner, described control method also comprise control be conveyed into described expansion system upstream contain heating in one of oxidant fluid and high-energy fluid or both contain the diluent fluid section.

209. such as the described control method of claim 187, also comprise and to be controlled at before leaving described burner and to be lower than 110% of the saturated level of described oxidant fluid that makes at the oxidant fluid that contains of described dilution with the diluent fluid section that contains that contains that oxidant fluid mixes.

210. such as the described control method of claim 197, wherein said heat and quality transmission system also comprise the blowdown exchanger that is positioned at described recompression machine downstream, what described control method comprised also that control flows through described blowdown exchanger contains the diluent fluid section, thus form heating contain the diluent fluid.

211. such as the described control method of claim 210, also the relative humidity of the discharging fluid of described energy conversion system is left in control, thereby impact forms the possibility of the column of smoke.

212. such as the described control method of claim 187, wherein said heat become with the quality delivery system configuration will vaporization the diluent fluid that contains be delivered to described burner, described method comprises that also control is conveyed into the vaporization diluent part in one of oxidant fluid and high-energy fluid or both of containing of described expansion system upstream.

213. such as the described control method of claim 187, wherein said heat becomes overheated vaporization diluent is delivered to described burner with the quality delivery system configuration, and described method comprises that also control is conveyed into the overheated vaporization diluent part in one of oxidant fluid and high-energy fluid or both of containing of described expansion system upstream.

214. such as the described control method of claim 187, also comprise and control the described diluent fluid that contains to the described conveying that contains oxidant fluid, wherein control the diluent degree of saturation that contains oxidant fluid of being carried by described oxidant delivery system.

215. such as the described control method of claim 187, comprise that also control is contained total diluent that the diluent fluid carries and contained the diluent fluid section that oxidant fluid is carried with described by described.

216. such as the described control method of claim 187, the wherein said oxidant fluid that contains is air, and the described diluent fluid that contains comprises water, and described control method comprises also that the water/AIR Proportional that will be delivered to described expansion system upstream is controlled at and is higher than 25% mass ratio.

217. such as the described control method of claim 187, described method comprises also that control is described and contains the distribution that the diluent fluid is carried, and the dilution dosage in the oxidant fluid of containing that wherein enters flame front in the described burner surpasses and makes the described saturated required dilution dosage of oxidant fluid that contains.

218. such as the described control method of claim 187, described method also comprises the distribution that the described diluent of control is carried, wherein given will contain oxidant fluid, contain the fluid fluid and contain under the respective conditions that the diluent fluid is delivered to described combustion system, if evenly mixing then the amount that contains oxidant fluid, contains the fluid fluid and contain the diluent fluid that forms described high-energy fluid can form incombustible mixture.

219. such as the described control method of claim 187, described method also comprise control described contain oxidant fluid carry and contain fuel fluid carry both one of or both control simultaneously, the extent of reaction in the wherein said burner is enough at least a non-oxidizable fuel element in the described discharging fluid is controlled at and is lower than desired concn.

220. such as the described control method of claim 187, described method also comprises the distribution that the described diluent of control is carried, the extent of reaction in the wherein said burner is enough to the side components in the described discharging fluid is controlled at and is lower than desired concn.

221. the method for control heat and dynamical system, described heat and dynamical system comprise:

Reactant delivery system, it is configured to carry the reaction-ure fluid that comprises reactant;

The co-reactant induction system, it is configured to carry the co-reactant fluid that comprises co-reactant;

The diluent induction system, it is configured to carry the diluent fluid that comprises the diluent of can vaporizing;

Reactor, it is configured to carry diluent, makes together reactant reaction and form high-energy fluid of reactant, and this high-energy fluid comprises the residual components of product, diluent and described co-reactant fluid and diluent fluid;

Decompressor, it is configured to make described high-energy fluid to expand and extracts mechanical energy, thereby forms expansion fluid;

The hot fluid heat exchanger, thus it is configured to that heat energy one of at least is recovered into the cooling agent fluid from described high-energy fluid and described expansion fluid and forms the fluid of heating and the fluid of cooling;

The component heat interchanger that is heated, it is configured to control the temperature of the described assembly that is heated and heat is recovered into the cooling agent fluid;

Controller, it is configured to control the conveying of described reaction-ure fluid, co-reactant fluid and diluent fluid;

Described method comprises:

Control described cooling agent fluid to the conveying of the described component heat interchanger that is heated, wherein the temperature of the described assembly that is heated is controlled at and is lower than selected temperature;

Control described diluent fluid to the described conveying that contains the high-energy fluid of co-reactant fluid or described decompressor outlet upstream, the peak temperature that wherein will enter the high-energy fluid of described decompressor is controlled at and is lower than assigned temperature;

Control the flow through conveying of described hot fluid heat exchanger of described cooling agent fluid, wherein reclaim heat from described high-energy fluid, and the temperature of the fluid of described heating is controlled at is higher than selected temperature;

Control the conveying of described reaction-ure fluid so that heat energy to be provided, described heat energy equals to be enough to carry the heat energy of the mechanical energy of being extracted by described decompressor at least from described high-energy fluid, add the summation of the heat energy that extracts from the high-energy fluid of described high-energy fluid or expansion and carried by described cooling agent fluid;

Control the one or both in described reaction-ure fluid and the described co-reactant fluid, so that described co-reactant belongs to the selected scope that be higher than a ratio and be lower than selected ratio with respect to stoichiometric co-reactant to the ratio λ of reactant ratio to reactant ratio;

The diluent of controlling in the described reactor is carried, and wherein controls nitrogen oxide from the expansion fluid that described energy conversion system is discharged and the amount of reaction contaminant component.

222. such as the described control method of claim 221, the fluid of wherein said heating comprises diluent.

223. such as the described control method of claim 221, wherein said reactant is the fuel that comprises in hydrogen and the carbon one or more.

224. such as the described control method of claim 221, wherein said co-reactant is one or more the oxidant that comprises in oxygen, fluorine, chlorine, bromine and the iodine.

225. such as the described temperature control method of claim 221, wherein said reactor configurations becomes can carry more than being enough to make the described diluent that contains the saturated amount of co-reactant fluid.

226. such as the described control method of claim 221, one of them receives heat to the wherein said assembly that is heated from described high-energy fluid and described expansion fluid, comprises one or more in described reactor assemblies, described decompressor assembly and the heat exchanger.

227. such as the described control method of claim 221, the wherein said assembly that is heated comprises the assembly of the inside heating that produces heat, and the assembly of wherein said inner heating comprises one or more in generator, motor, bearing, thermo-mechanical drive and electromagnetic transducer and the electromagnetic controller.

228. such as the described control method of claim 227, also comprise and carry the diluent of heating to cool off other assembly that is heated.

229. such as the described control method of claim 227, comprise that also the diluent with heating is delivered to the heat application.

230. such as the described control method of claim 227, comprise that also the diluent with heating is delivered to described reactor.

231. the method for switching energy in energy conversion system, described energy conversion system comprises:

Use oxidant delivery system to carry the method for oxidant, described oxidant delivery system has entrance and exit, and it is configured to be conveyed into described energy conversion system with containing oxidant fluid;

Use the method for fuel delivery system transfer the fuel, described fuel delivery system is configured to be conveyed into described energy conversion system with containing fuel fluid;

Use the diluent induction system to carry the method for diluent, described diluent induction system is configured to carry and contains the diluent fluid in the described energy conversion system, at least part of described diluent fluid that contains comprises vaporizable diluent fluid, and wherein at least part of diluent fluid that contains is pressurised into liquid state;

Use the method for combustion system burning, described combustion system is configured to receive fluid from described fuel delivery system, described oxidant delivery system and described diluent induction system; And comprise the combustion chamber, described combustion chamber has at least one and exports the entrance that exists fluid to be communicated with described oxidant delivery system outlet and described fuel delivery system; Has at least one outlet, described combustion system is configured to mix containing fuel fluid and containing oxidant fluid, to form flammable fuel and oxidant mixture, thereby and with oxidant fuel is carried out oxidation and form oxidation product, and at least part of liquid state is contained the diluent fluid deliver into described combustion chamber; Described combustion system also is configured to carry and mixes and contains the diluent fluid and contain oxidant fluid, contain a kind of and multiple in fuel fluid and the oxidation product; The peak temperature of the high-energy fluid of described combustion system is left in restriction; And formation comprises the high-energy fluid of the diluent fluid of oxidation product and vaporization in described combustion system, and has one or more level to raise among the temperature of described high-energy fluid, pressure and the kinetic energy;

The method of using expansion system to expand, described expansion system comprises the decompressor with entrance and exit, it is configured to make at least part of described high-energy fluid to expand, thereby forms expansion fluid;

With the method that heat and quality transmission system are carried out heat and quality transmission, described heat and quality transmission system have a plurality of entrance and exits, and it is configured to: thus from described expansion fluid, reclaim the expansion fluid that heat forms cooling; Thereby provide heat to form the diluent fluid of heating to the described diluent fluid that contains; Be delivered to the diluent fluid of the heating of small part to described combustion system;

Reclaim the method for diluent with the diluent recovery system, described diluent recovery system is configured to reclaim diluent from described expansion fluid, and described yield is at least about equaling to be conveyed into the oxidant fluid of described expansion system outlet upstream or the amount in the high-energy fluid; And recovery section water, described water be following both one of or both combinations: the water that forms in the combustion process and together be conveyed into the water of described oxidant delivery system with described oxidant fluid;

Process the method for fluid with the fluid treatment system, described fluid treatment system is configured to at least a portion that removes the water that reclaims from described expansion fluid, wherein remove the part of at least a alloy in the described expansion fluid, and reduce the concentration of this alloy of the high-energy fluid that enters described expansion system.

Images